CN219783836U - Fusel oil continuous separation device - Google Patents
Fusel oil continuous separation device Download PDFInfo
- Publication number
- CN219783836U CN219783836U CN202320677668.4U CN202320677668U CN219783836U CN 219783836 U CN219783836 U CN 219783836U CN 202320677668 U CN202320677668 U CN 202320677668U CN 219783836 U CN219783836 U CN 219783836U
- Authority
- CN
- China
- Prior art keywords
- tower
- fractionating
- fractionating tower
- water diversion
- water
- 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
- 239000001760 fusel oil Substances 0.000 title claims abstract description 37
- 238000000926 separation method Methods 0.000 title claims abstract description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 131
- 239000002516 radical scavenger Substances 0.000 claims abstract description 14
- 238000005194 fractionation Methods 0.000 claims description 15
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical group O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 9
- 229920006395 saturated elastomer Polymers 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 2
- 239000000463 material Substances 0.000 abstract description 9
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 238000000034 method Methods 0.000 abstract description 5
- 239000002699 waste material Substances 0.000 abstract description 5
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 238000011031 large-scale manufacturing process Methods 0.000 abstract description 3
- 238000011084 recovery Methods 0.000 abstract description 3
- PHTQWCKDNZKARW-UHFFFAOYSA-N isoamylol Chemical compound CC(C)CCO PHTQWCKDNZKARW-UHFFFAOYSA-N 0.000 description 22
- ZXEKIIBDNHEJCQ-UHFFFAOYSA-N isobutanol Chemical compound CC(C)CO ZXEKIIBDNHEJCQ-UHFFFAOYSA-N 0.000 description 20
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 15
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 9
- QPRQEDXDYOZYLA-UHFFFAOYSA-N 2-methylbutan-1-ol Chemical compound CCC(C)CO QPRQEDXDYOZYLA-UHFFFAOYSA-N 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 6
- 239000007788 liquid Substances 0.000 description 6
- 238000010992 reflux Methods 0.000 description 6
- 238000009835 boiling Methods 0.000 description 5
- 238000005086 pumping Methods 0.000 description 5
- IWTBVKIGCDZRPL-LURJTMIESA-N 3-Methylbutanol Natural products CC[C@H](C)CCO IWTBVKIGCDZRPL-LURJTMIESA-N 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 150000001298 alcohols Chemical class 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000002304 perfume Substances 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000796 flavoring agent Substances 0.000 description 1
- 235000019634 flavors Nutrition 0.000 description 1
- 235000021190 leftovers Nutrition 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model discloses a fusel oil continuous separation device, which comprises a fractionating tower and a water diversion tower, wherein the fractionating tower comprises a first fractionating tower, a second fractionating tower, a third fractionating tower and a fourth fractionating tower, the water diversion tower comprises a first water diversion tower, a second water diversion tower and a third water diversion tower, the first fractionating tower is connected with the second fractionating tower through the first water diversion tower, the second fractionating tower is connected with the third fractionating tower through the second water diversion tower, and the third fractionating tower is connected with the fourth fractionating tower through the third water diversion tower; and the second water diversion tower and the third water diversion tower are respectively provided with a water scavenger inlet for adding a water scavenger into the second water diversion tower and the third water diversion tower. By arranging a plurality of fractionating towers for continuously separating fusel oil, the steam consumption can be saved by at least 40% compared with the original process, and the energy consumption is reduced; the method has the advantages of no intermediate materials, no need of a large number of intermediate tanks for storage, production cost reduction, short treatment period, large-scale production and production efficiency improvement; the recovery rate of each material in the fusel oil is high, and the waste is avoided.
Description
Technical Field
The utility model relates to the technical field of edible flavors, in particular to a fusel oil continuous separation device.
Background
Fusel oil isThe main component of the leftovers generated by fermenting alcohol is C 2 -C 5 Comprises 45% of isoamyl alcohol, 9% of isobutanol, 1.3% of propanol, 20% of ethanol and 24% of water. These alcohols are basic raw materials for preparing natural equivalent perfume aldehydes, acids and esters in the perfume industry, and have a large market gap. Ethanol, propanol and water in the fusel oil are mutually soluble; the solubility of the isobutanol and the isoamyl alcohol in water is high; and these alcohols and water can form azeotropes; the content of the propanol and the isobutanol is lower. The prior fusel oil separation process mainly adopts intermittent repeated fractionation, and repeatedly uses brine or alkali (sodium hydroxide) water for dewatering, re-fractionation and purification.
However, in the process of implementing the technical scheme of the embodiment of the present utility model, the present inventors have found that at least the following problems exist in the above-mentioned technology:
the repeated fractionation has the problems of high energy consumption, long treatment period and difficult mass production, and the repeated fractionation also causes too many intermediate materials, a large number of intermediate tanks are needed, so that the production cost is greatly increased; in addition, the extraction rate of propanol and isobutanol is low, the waste materials are more, and the waste is serious.
Disclosure of Invention
The utility model aims to provide a fusel oil continuous separation device, which solves the technical problems in the background art, and is realized by the following technical scheme:
the continuous fusel oil separation device comprises a fractionating tower and a water diversion tower, wherein the fractionating tower comprises a first fractionating tower, a second fractionating tower, a third fractionating tower and a fourth fractionating tower, the water diversion tower comprises a first water diversion tower, a second water diversion tower and a third water diversion tower, the first fractionating tower is connected with the second fractionating tower through the first water diversion tower, the second fractionating tower is connected with the third fractionating tower through the second water diversion tower, and the third fractionating tower is connected with the fourth fractionating tower through the third water diversion tower; and the second water diversion tower and the third water diversion tower are respectively provided with a water scavenger inlet for adding a water scavenger into the second water diversion tower and the third water diversion tower.
Further, a top discharge hole, a bottom discharge hole and a feeding hole in the tower are arranged on the fractionating tower, and a feeding hole, a discharge hole and a water outlet are arranged on the water diversion tower.
Further, a feeding hole in the tower of the first fractionating tower is communicated with a fusel oil storage tank, and a discharging hole at the bottom of the first fractionating tower is communicated with a feeding hole of the first water diversion tower; the discharge port of the first water diversion tower is communicated with the feeding port in the second water diversion tower, and the discharge port at the top of the second water diversion tower is communicated with the feeding port of the second water diversion tower; the discharge port of the second fractionating tower is communicated with the feed port in the third fractionating tower, and the top discharge port of the third fractionating tower is communicated with the feed port of the third fractionating tower; the discharge port of the third diversion tower is communicated with the feeding port in the tower of the fourth fractionating tower, and the top discharge port of the fourth fractionating tower is communicated with the feeding port of the third diversion tower.
Further, the temperature of the top of the first fractionating tower is less than or equal to 79 ℃, and the temperature of the bottom of the first fractionating tower is more than or equal to 88 ℃; the temperature of the top of the second fractionating tower is less than or equal to 90 ℃, and the temperature of the bottom of the second fractionating tower is more than or equal to 129 ℃; the temperature of the top of the third fractionating tower is less than or equal to 87 ℃, and the temperature of the bottom of the third fractionating tower is more than or equal to 107 ℃; the temperature of the top of the fourth fractionating tower is less than or equal to 80 ℃, and the temperature of the bottom of the fourth fractionating tower is more than or equal to 98 ℃.
Further, the continuous separation device also comprises a fifth fractionating tower, and a bottom discharge hole of the second fractionating tower is communicated with a feeding hole in the fifth fractionating tower.
Further, the temperature of the top of the fifth fractionating tower is less than or equal to 129 ℃, and the temperature of the bottom of the fifth fractionating tower is more than or equal to 132 ℃.
Further, the water scavenger is saturated brine or saturated alkaline water.
The technical scheme provided by the embodiment of the utility model has at least the following technical effects or advantages:
1. by arranging a plurality of fractionating towers for continuously separating fusel oil, the steam consumption can be saved by at least 40% compared with the original process, and the energy consumption is reduced;
2. the fusel oil is continuously separated by arranging a plurality of fractionating towers, so that intermediate materials are not needed, a large amount of intermediate tanks for storage are not needed, the production cost is reduced, the treatment period is short, the large-scale production can be realized, and the production efficiency is improved;
3. the recovery rate of each material in the fusel oil is high and almost reaches 100%, so that the waste is avoided.
Drawings
The accompanying drawings, which are included to provide a further understanding of the utility model and are incorporated in and constitute a part of this specification, illustrate embodiments of the utility model and together with the description serve to explain the utility model.
FIG. 1 is a schematic diagram of an embodiment of the present utility model.
The symbols in the drawings are: 1. a first fractionation column; 2. a first water diversion tower; 3. a second fractionation column; 4. a second water separation tower; 5. a third fractionation column; 6. a third water diversion tower; 7. a fourth fractionation column; 8. and a fifth fractionating tower.
Detailed Description
In order that the manner in which the above recited features of the present utility model can be better understood, a more particular description of the utility model will be rendered by reference to specific embodiments thereof which are illustrated in the appended drawings. The following description of at least one exemplary embodiment is merely exemplary in nature and is in no way intended to limit the utility model, its application, or uses. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
A fusel oil continuous separation device shown in figure 1 comprises a fractionating tower and a water diversion tower, wherein a top discharge hole, a bottom discharge hole and a feeding hole in the tower are arranged on the fractionating tower, and a feeding hole, a discharge hole and a water discharge hole are arranged on the water diversion tower. Wherein the fractionating tower comprises a first fractionating tower 1, a second fractionating tower 3, a third fractionating tower 5, a fourth fractionating tower 7 and a fifth fractionating tower 8, and the water diversion tower comprises a first water diversion tower 2, a second water diversion tower 4 and a third water diversion tower 6.
Specifically, the feed inlet in the column of the first fractionation column 1 communicates with a fusel oil reservoir (not shown) for adding fusel oil to the first fractionation column 1. The bottom discharge port of the first fractionating tower 1 is communicated with the feed inlet of the first water diversion tower 2 through a pipeline. The temperature of the top of the first fractionating tower 1 is less than or equal to 79 ℃, and the temperature of the bottom of the first fractionating tower 1 is more than or equal to 88 ℃, so that ethanol in fusel oil is separated and extracted from a top discharge port of the first fractionating tower 1, and the residual components of the fusel oil enter the first water knockout tower 2 from a bottom discharge port of the first fractionating tower 1.
The discharge port of the first diversion tower 2 is communicated with the feed port in the tower of the second diversion tower 3, an oil layer in fusel oil enters the second diversion tower 3 from the discharge port at the upper end of the first diversion tower 2, and a water layer in fusel oil is discharged from the water outlet at the lower end of the first diversion tower 2.
The top outlet of the second fractionating tower 3 is communicated with the inlet of the second fractionating tower 4 through a pipeline, the top temperature of the second fractionating tower 3 is less than or equal to 90 ℃, the bottom temperature of the second fractionating tower 3 is less than or equal to 129 ℃, and isobutanol and propanol in fusel oil are extracted from the top outlet of the second fractionating tower 3 and are fed into the second fractionating tower 4. The discharge port of the second water diversion tower 4 is communicated with the feeding port in the third fractionating tower 5, the oil layer enters the third fractionating tower 5 from the discharge port at the top of the second water diversion tower 4, and the water layer is discharged from the water outlet at the lower end of the second water diversion tower 4. Wherein, the second water diversion tower 4 is also provided with a water scavenger inlet for adding a water scavenger into the second water diversion tower 4. Preferably, the water scavenger is saturated brine or saturated alkaline water, so as to remove a large amount of water in the oil layer and reduce the solubility of isobutanol and propanol in water.
The bottom discharge port of the second fractionating tower 3 is communicated with the feeding port in the fifth fractionating tower 8 through a pipeline, so that isoamyl alcohol in fusel oil enters the fifth fractionating tower 8 from the bottom discharge port of the second fractionating tower 3 through the feeding port in the fifth fractionating tower 8, the top temperature of the fifth fractionating tower 8 is less than or equal to 129 ℃, the bottom temperature of the fifth fractionating tower 8 is more than or equal to 132 ℃, the isoamyl alcohol is further separated into 2-methyl butanol and 3-methyl butanol, 2-methyl butanol is extracted from the top discharge port of the fifth fractionating tower 8, and 3-methyl butanol is extracted from the bottom discharge port of the fifth fractionating tower 8.
The top discharge port of the third fractionating tower 5 is communicated with the feed port of the third water diversion tower 6 through a pipeline. The temperature of the top of the third fractionating tower 5 is less than or equal to 87 ℃, and the temperature of the bottom of the third fractionating tower 5 is more than or equal to 107 ℃ so as to realize the separation of the isobutanol and the propanol. The propanol and water are extracted from the top outlet of the third fractionating tower 5 and are fed into the third water diversion tower 6, and the isobutanol is extracted from the bottom outlet of the third fractionating tower 5.
The discharge port of the third diversion tower 6 is communicated with the feed port in the tower of the fourth fractionating tower 7, an oil layer enters the fourth fractionating tower 7 from the discharge port at the top of the third diversion tower 6, and a water layer is discharged from the water outlet at the bottom of the third diversion tower 6. The third water diversion tower 6 is also provided with a water scavenger inlet for adding a water scavenger into the third water diversion tower 6. Preferably, the water scavenger is saturated brine or saturated alkaline water, thereby removing a large amount of water in the oil layer and reducing the solubility of propanol in water.
The top outlet of the fourth fractionating tower 7 is communicated with the feed inlet of the third water diversion tower 6 through a pipeline, the top temperature of the fourth fractionating tower 7 is less than or equal to 80 ℃, the bottom temperature of the fourth fractionating tower 7 is more than or equal to 98 ℃, the bottom outlet of the fourth fractionating tower 7 is used for extracting propanol, and the non-separated propanol returns to the third water diversion tower 6 for circulating separation.
The working principle of the embodiment of the utility model is as follows:
pumping the fusel oil with the clear water separated into a first fractionating tower to a certain liquid level at the bottom of the tower, heating and refluxing for 2 hours by boiling the steam in a boiling device, feeding the fusel oil when the temperature of the tower top reaches 77 ℃ and the temperature of the tower bottom reaches more than 88 ℃, extracting ethanol (the content is about 95%) from the top of the first fractionating tower, and feeding the tower bottom material into a first water diversion tower from a discharge hole at the bottom of the first fractionating tower;
when the liquid level of the first diversion tower reaches the middle position of the tower, a water outlet at the bottom of the first diversion tower is opened, and the oil-water interface is controlled to be always at 1/4 position at the bottom of the first diversion tower by adjusting a water valve at the water outlet;
pumping an oil layer at the top of the first water diversion tower into a second fractionating tower to reach a certain liquid level at the bottom of the tower, heating and refluxing for 2 hours by boiling steam, feeding the oil layer after the temperature of the top of the tower reaches 89 ℃ and the temperature of the bottom of the tower reaches 129 ℃ or higher, extracting azeotrope (mainly containing propanol, isobutanol and water) from the top of the second fractionating tower, and feeding the bottom material (isoamyl alcohol) into a fifth fractionating tower from a discharge hole at the bottom of the second fractionating tower;
and (3) when the azeotrope at the top of the second fractionating tower enters the second fractionating tower, opening saturated brine into the second fractionating tower, and keeping the flow rate of the two substantially consistent. Opening a water outlet at the bottom of the second water diversion tower, and controlling an oil-water interface to be always at a position 1/4 of the bottom of the second water diversion tower by adjusting a water valve;
pumping an oil layer at the top of the second fractionating tower into a third fractionating tower to reach a certain liquid level at the bottom of the tower, heating and refluxing for 2h by boiling steam, feeding the oil layer after the temperature of the top of the tower reaches 87 ℃ and the temperature of the bottom of the tower reaches more than 107 ℃, extracting azeotrope (mainly containing propanol and water) from the top of the third fractionating tower, and extracting isobutanol from a discharge port at the bottom of the third fractionating tower;
and (3) enabling the azeotrope at the top of the third fractionating tower to enter the third water diversion tower, and simultaneously enabling the open saturated brine to enter the third water diversion tower, so that the flow rates of the open saturated brine and the open saturated brine are basically consistent. A water outlet at the bottom of the third water diversion tower is opened, and an oil-water interface is controlled to be always at 1/4 position at the bottom of the third water diversion tower by adjusting a water valve;
pumping an oil layer at the top of the third fractionating tower into a fourth fractionating tower to reach a certain liquid level at the bottom of the tower, heating and refluxing for 2 hours by boiling steam, feeding the oil layer after the top temperature reaches 87 ℃ and the bottom temperature reaches more than 98 ℃, extracting azeotrope (mainly containing propanol and water) at the top of the fourth fractionating tower, returning the azeotrope to the third fractionating tower, and extracting propanol at the bottom of the fourth fractionating tower;
pumping isoamyl alcohol at the bottom of the second fractionating tower into a fifth fractionating tower to reach a certain liquid level at the bottom of the tower, heating and refluxing the isoamyl alcohol by opening a boiler for 15 hours, heating and refluxing the isoamyl alcohol until the top temperature reaches 128 ℃ (the GC is used for detecting the 3-methyl butanol and is less than or equal to 0.5 percent), the bottom temperature reaches 132 ℃ (the GC is used for detecting the 2-methyl butanol and is less than or equal to 0.5 percent), feeding the isoamyl alcohol into an oil layer, extracting the 2-methyl butanol from the top of the fifth fractionating tower, and extracting the 3-methyl butanol from the bottom of the fifth fractionating tower.
Wherein, the temperature of the top and the bottom of the fractionating tower can be strictly controlled by adjusting the discharge amount of the top and the bottom of the fractionating tower, so that the temperature is stabilized in a specified range.
The technical scheme provided by the embodiment of the utility model at least has the following technical effects or advantages:
1. by arranging a plurality of fractionating towers for continuously separating fusel oil, the steam consumption can be saved by at least 40% compared with the original process, and the energy consumption is reduced;
2. the fusel oil is continuously separated by arranging a plurality of fractionating towers, so that intermediate materials are not needed, a large amount of intermediate tanks for storage are not needed, the production cost is reduced, the treatment period is short, the large-scale production can be realized, and the production efficiency is improved;
3. the recovery rate of each material in the fusel oil is high and almost reaches 100%, so that the waste is avoided.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the present utility model. As used herein, the singular is also intended to include the plural unless the context clearly indicates otherwise, and furthermore, it is to be understood that the terms "comprises" and/or "comprising" when used in this specification are taken to specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof.
In addition, the terms "first", "second", etc. are used to define the components, and are only for convenience of distinguishing the corresponding components, and the terms have no special meaning unless otherwise stated, and therefore should not be construed as limiting the scope of the present utility model.
The above description is only of the preferred embodiments of the present utility model and is not intended to limit the present utility model, but various modifications and variations can be made to the present utility model by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present utility model should be included in the protection scope of the present utility model.
Claims (7)
1. The continuous fusel oil separation device comprises a fractionating tower and a water diversion tower, and is characterized in that the fractionating tower comprises a first fractionating tower, a second fractionating tower, a third fractionating tower and a fourth fractionating tower, the water diversion tower comprises a first water diversion tower, a second water diversion tower and a third water diversion tower, the first fractionating tower is connected with the second fractionating tower through the first water diversion tower, the second fractionating tower is connected with the third fractionating tower through the second water diversion tower, and the third fractionating tower is connected with the fourth fractionating tower through the third water diversion tower; and the second water diversion tower and the third water diversion tower are respectively provided with a water scavenger inlet used for adding a water scavenger into the second water diversion tower and the third water diversion tower.
2. The continuous fusel oil separation device according to claim 1, wherein the fractionating tower is provided with a top outlet, a bottom outlet and a feeding inlet in the tower, and the water diversion tower is provided with a feeding inlet, a discharging outlet and a water outlet.
3. The continuous fusel oil separation device of claim 2, wherein a column feed inlet of the first fractionation column is in communication with a fusel oil storage tank, and a column bottom discharge outlet of the first fractionation column is in communication with a feed inlet of the first water knockout column; the discharge port of the first water diversion tower is communicated with the feed port in the second water diversion tower, and the top discharge port of the second water diversion tower is communicated with the feed port of the second water diversion tower; the discharge port of the second fractionating tower is communicated with the feeding port in the third fractionating tower, and the top discharge port of the third fractionating tower is communicated with the feeding port of the third fractionating tower; the discharge port of the third water diversion tower is communicated with the feeding port in the tower of the fourth fractionating tower, and the top discharge port of the fourth fractionating tower is communicated with the feeding port of the third water diversion tower.
4. The fusel oil continuous separation device according to claim 1, wherein the top temperature of the first fractionating tower is equal to or less than 79 ℃, and the bottom temperature of the first fractionating tower is equal to or more than 88 ℃; the temperature of the top of the second fractionating tower is less than or equal to 90 ℃, and the temperature of the bottom of the second fractionating tower is more than or equal to 129 ℃; the temperature of the top of the third fractionating tower is less than or equal to 87 ℃, and the temperature of the bottom of the third fractionating tower is more than or equal to 107 ℃; the temperature of the top of the fourth fractionating tower is less than or equal to 80 ℃, and the temperature of the bottom of the fourth fractionating tower is more than or equal to 98 ℃.
5. A fusel oil continuous separation apparatus as in claim 3, further comprising a fifth fractionation column, wherein the bottom outlet of the second fractionation column is in communication with the in-column inlet of the fifth fractionation column.
6. The continuous fusel oil separator of claim 5, wherein the top temperature of the fifth fractionating tower is less than or equal to 129 ℃, and the bottom temperature of the fifth fractionating tower is less than or equal to 132 ℃.
7. The continuous fusel oil separator of claim 1, wherein the water scavenger is saturated brine or saturated alkaline water.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320677668.4U CN219783836U (en) | 2023-03-31 | 2023-03-31 | Fusel oil continuous separation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320677668.4U CN219783836U (en) | 2023-03-31 | 2023-03-31 | Fusel oil continuous separation device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN219783836U true CN219783836U (en) | 2023-10-03 |
Family
ID=88154227
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202320677668.4U Active CN219783836U (en) | 2023-03-31 | 2023-03-31 | Fusel oil continuous separation device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN219783836U (en) |
-
2023
- 2023-03-31 CN CN202320677668.4U patent/CN219783836U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101955828A (en) | Method for removing hydrogen sulfide from natural gas | |
| CN102399130A (en) | Method for simplifying rectification process for preparing ethanol through hydrogenation of acetic acid | |
| CN101717163A (en) | Method for processing methanol rectified raffinate | |
| CN102618383B (en) | Production method and system of deacidification rice bran oil | |
| CN219783836U (en) | Fusel oil continuous separation device | |
| CN202478767U (en) | Vinyl chloride dehydration device | |
| CN110698325A (en) | Production device and process for co-producing fuel ethanol and special grade edible alcohol | |
| CN210751350U (en) | Automatic continuous extraction device for obtaining white spirit seasoning from white spirit brewing byproduct yellow water | |
| CN109609284B (en) | Process and system for extracting oil from waste clay | |
| CN1114458C (en) | Crude oil atmospheric vacuum distillation method with deep stripping process | |
| CN113620804A (en) | Continuous esterification process and device for ethyl 2-methylbutyrate | |
| CN104911025A (en) | Technique for preparing oil by leaching tea seed cake | |
| CN101475889B (en) | Method for extracting spirit natural fermentation by-product by supercritical carbon dioxide | |
| CN210765250U (en) | Automatic continuous extraction device for obtaining raw wine from white spirit brewing by-product yellow water | |
| CN209759075U (en) | Adsorption interception oil-water separation deoiling device | |
| CN209173636U (en) | Nicotine steam purge device when using tobacco waste extraction nicotine | |
| CN203002028U (en) | Novel phase separator for removing water in difluoromono chloroethane | |
| CN202336224U (en) | Azeotropic distillation system for mixture of carbinol and tetrahydrofuran | |
| CN102604746B (en) | Production system for extracting industrial waste grease from swill-cooked dirty oil | |
| CN212467173U (en) | Low-boiling ester and glycerin separation device for biodiesel distillation process | |
| CN202322785U (en) | Waste animal and vegetable oil reclaiming system | |
| CN102875353B (en) | Method for extracting acetic acid from carbon-soot-containing acetic acid water solution through dust removal/side-stream discharge/azeotropic rectification | |
| CN209636198U (en) | A kind of spent bleaching clay mentions oil system | |
| CN203469516U (en) | Device for recycling xylene in camphor synthesized by using ester-soap method | |
| CN216639346U (en) | Sodium carboxymethylcellulose production ethanol recycle device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |