CN201567322U - Vegetable oil and fat desolventizing tower - Google Patents
Vegetable oil and fat desolventizing tower Download PDFInfo
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- CN201567322U CN201567322U CN2009202584897U CN200920258489U CN201567322U CN 201567322 U CN201567322 U CN 201567322U CN 2009202584897 U CN2009202584897 U CN 2009202584897U CN 200920258489 U CN200920258489 U CN 200920258489U CN 201567322 U CN201567322 U CN 201567322U
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Abstract
The utility model discloses a vegetable oil and fat desolventizing tower, consisting of a vertical closed tower body; the tower body comprises a water-steam trapping section, a steam stripping section and a tower-kettle section from top to bottom; the water-steam trapping section is internally provided with packing; the steam stripping section consists of a distributing disc, a packing layer and a collecting layer; and the upper end of the steam stripping section is provided with a spraying pipe which is communicated with the distributing disc; and the bottom end of the tower-kettle section is provided with a steam-spraying pipe, and the lower end thereof is connected with a finished oil discharging section. The vegetable fat desolventizing tower consists of the water-steam trapping section, the steam stripping section and the tower-kettle section which are integrated into a whole so as to lead the equipment to have compact structure and small occupying area. In addition, the vegetable fat desolventizing tower has the following advantages that: 1. the film mass-transfer theory is adopted, and an oil phase has large surface area, thus improving the water-steam mass-transfer efficiency, and saving the steam stripping and steam consumption; and 2. the oil and fat removes a solvent component at lower temperature and in shorter time, thus avoiding the formation of trans-acid influencing the body health; and the oil product has stable quality.
Description
Technical field
The utility model belongs to the chemical industry equipment of a vegetable oil precipitation, relates to a vegetable oil precipitation tower specifically.
Background technology
The many tank body formulas of domestic existing Vegetable oil lipoprotein desolventizing equipment based on the band traverse baffle, such equipment is the following problem of ubiquity in use: vegetables oil removes the temperature of solvent must be more than 140 ℃, the time that oil stops in jar long (about 2h), high temperature can influence oil quality for a long time, and nutritive value also can reduce.Require equipment must have enough big volume simultaneously, cause the consumption of vacuum system steam to increase.In addition, the realization of steam distillation (stripping) is to spray into open steam by some nozzles in oil reservoir, oil reservoir is produced seethe that the vapour-liquid contact area realizes to increase.The fresh stripped vapor that sprays into only contacts with oil and once promptly leaves tank body, and stripped vapor fails to be fully used, vapour-liquid contact weak effect, and grease precipitation efficient is low; In addition, the precipitation jar is because phenomenons such as splashing of producing when directly vapour sprays into, liquid flooding make the refining consumption increase.
Summary of the invention
The utility model has solved the precipitation jar, and precipitation temperature height, the residence time are grown in jar, oil quality is poor, steam consumption quantity is big, equipment volume is huge, the high shortcoming of refining consumption, a kind of vapour-liquid mass efficient height is provided, saves stripping and vacuum system steam consumption and the stable Vegetable oil lipoprotein precipitation tower of oil quality.
For achieving the above object, the utility model is by the following technical solutions:
The utility model is made of vertical sealing tower body, and above-mentioned tower body comprises that from top to bottom vapour-liquid captures section, stripping stage and tower still section; Above-mentioned vapour-liquid captures in the section and is provided with filler; Above-mentioned stripping stage is made of distribution plate, packing layer and collecting layer from top to bottom, is provided with shower in the upper end of stripping stage, and shower communicates with distribution plate; Bottom in tower still section is provided with the vapour jet pipe, and the lower end of tower still section connects processed oil and discharges section.
Above-mentioned vapour-liquid captures section and stripping stage is solidified as a whole, and its diameter is Φ 400～600mm; The diameter of above-mentioned tower still section is Φ 1100～1300mm.
Above-mentioned filler is a Stainless Steel Wire.
Above-mentioned packing layer is the stainless steel orifice plate.
Top in tower still section is provided with the gas evolution mouth.
In processed oil discharge section, be provided with the oil level detection control device.
Adopt the utility model of technique scheme, capture section, stripping stage and tower still section by vapour-liquid and form, three parts are as a whole mutually, make compact equipment, and floor space is little.In addition, the utility model waits other legacy equipments to compare with the precipitation jar and has the following advantages: (1) adopts the thin film mass transfer theory, and oil phase has huge surface-area, has improved vapour-liquid mass efficient, save the steam consumption of stripping and vacuum system, can save steam 50%-70%; (2) grease is in relatively low temperature with remove solvent composition in the short period, avoided influencing the formation of the trans acids of HUMAN HEALTH, and oil quality is stable; (3) equipment is simple, compact construction, reduced investment; (4) also can carry out the operation that grease dehydrates with this tower.
Description of drawings
Accompanying drawing is an one-piece construction synoptic diagram of the present utility model.
Embodiment
As shown in the figure, the utility model is made of vertical sealing tower body, and it is as a whole mutually that this vertical sealing tower body comprises that from top to bottom vapour-liquid captures section 1, stripping stage 2 and tower still section 3, three parts, makes compact equipment, and floor space is little.
Above-mentioned vapour-liquid captures in the section 1 and is provided with filler 11, and this filler 11 is a Stainless Steel Wire, and the top is provided with vacuum interface 9, and vacuum interface 9 connects vacuum system.
The lower end that vapour-liquid captures section 1 connects stripping stage 2, and stripping stage 2 is the main part of tower, and solvent in the oil product and volatilization component are mainly removed in this section.Stripping stage 2 is made of distribution plate 4, packing layer 5 and collecting layer 6 from top to bottom, is provided with shower 10 in the upper end of stripping stage 2, and shower 10 communicates with distribution plate 4, and above-mentioned distribution plate 4 is the divider of disc type.It is pointed out that packing layer 5 is regular stainless steel orifice plate.
The lower end of stripping stage 2 connects tower still section 3, grease behind the tower still section 3 main collection precipitations, the liquid level that keeps normal running, simultaneously gas evolution mouth 8 is set on the top of tower still section 3, its bottom is provided with vapour jet pipe 7, and the lower end of tower still section 3 connects processed oil and discharges section 12, discharges in the section 12 at processed oil and is provided with the oil level detection control device, guarantee that oil is not evacuated, thus the destruction that can not cause vacuum system.
In the preparation, vapour-liquid captures section 1 and stripping stage 2 can be solidified as a whole, specifically, the barrel diameter of vapour-liquid capture section 1 is any one among Φ 400, Φ 500, the Φ 600, filler 11 is regular stainless steel orifice plate, capture section top and have the vacuum interface 9 of Φ 100mm, the high filler of 200mm 11 is arranged at the interface bottom, prevents that drop from being taken away by vacuum system.Packing layer 5 in the stripping stage 2 highly is 2000mm, and oil sprays into distribution plate 4 from upper spray pipe 10, and the tubing diameter that connects shower 10 and distribution plate 4 is Φ 57mm.The barrel diameter of above-mentioned tower still section 3 is any one among Φ 1100, Φ 1200, the 1300mm, and it highly is 1600mm, and respectively there are the high end socket of 300mm in upper strata and lower floor, and whole tower body height is 7500mm; Oil total residence time in tower is 15min.
Working process of the present utility model is as follows:
The vegetables oil for the treatment of precipitation enters distribution plate 4 from stripping stage 2 tops, after distributing, distribution plate 4 evenly flows through packing layer 5 surfaces from top to bottom, and directly carry out mass transfer with steam that tower still section 3 upper gas escape orifices 8 rise, promptly steam distillation comes out solvent in the oil and other volatilization component stripping.Because packing layer 5 itself has bigger surface-area, thereby heat transfer coefficient is big, rate of mass transfer is fast, can save the straying quatity of open steam, greatly reduce the volatilization time of solvent component, thereby shortened the precipitation time, increase greasy stability in storage, guaranteed oil quality.Stripping stage 2 strippings go out to volatilize and discharge after component enters stripping stage top vapour-liquid capture section 1 capture drop.In addition, grease is not that intensive impacts with contacting of steam in the tower, has avoided the splash loss of oil of cat head, and refining consumes corresponding reduction.The oil that gets off from stripping stage 2 enters tower still section 3, carries out contacting the first time at this live steam and grease, thereby realizes counter-current operation, has guaranteed the effect of grease precipitation.The utility model is owing to adopted the thin film mass transfer theory, and when guaranteeing the precipitation effect, making its service temperature is 115--120 ℃, has reduced service temperature, and has significantly shortened the precipitation time, is 10-15min only, thereby has improved the precipitation efficient of Vegetable oil lipoprotein.
Claims (6)
1. Vegetable oil lipoprotein precipitation tower, it is characterized in that: it is made of vertical sealing tower body, and described tower body comprises that from top to bottom vapour-liquid captures section (1), stripping stage (2) and tower still section (3); Described vapour-liquid captures in the section (1) and is provided with filler (11); Described stripping stage (2) by distribution plate (4), packing layer (5) and collecting layer (6) formation, is provided with shower (10) in the upper end of stripping stage (2) from top to bottom, and shower (10) communicates with distribution plate (4); In the bottom of described tower still section (3) vapour jet pipe (7) is set, the lower end of tower still section (3) connects processed oil and discharges section (12).
2. Vegetable oil lipoprotein precipitation tower according to claim 1 is characterized in that: described vapour-liquid captures section (1) and stripping stage (2) is solidified as a whole, and its diameter is Φ 400～600mm; The diameter of described tower still section (3) is Φ 1100～1300mm.
3. Vegetable oil lipoprotein precipitation tower according to claim 1 is characterized in that: described filler (11) is a Stainless Steel Wire.
4. Vegetable oil lipoprotein precipitation tower according to claim 1 is characterized in that: described packing layer (5) is the stainless steel orifice plate.
5. according to the arbitrary described Vegetable oil lipoprotein precipitation tower of claim 1～4, it is characterized in that: be provided with gas evolution mouth (8) on the top of described tower still section (3).
6. Vegetable oil lipoprotein precipitation tower according to claim 5 is characterized in that: discharge in the section (12) at described processed oil and be provided with the oil level detection control device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202584897U CN201567322U (en) | 2009-11-26 | 2009-11-26 | Vegetable oil and fat desolventizing tower |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202584897U CN201567322U (en) | 2009-11-26 | 2009-11-26 | Vegetable oil and fat desolventizing tower |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201567322U true CN201567322U (en) | 2010-09-01 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009202584897U Expired - Fee Related CN201567322U (en) | 2009-11-26 | 2009-11-26 | Vegetable oil and fat desolventizing tower |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201567322U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104327946A (en) * | 2014-10-31 | 2015-02-04 | 新疆正企生物科技有限公司 | Purification device and process for crude cotton seed oil produced by leaching process |
| CN108373944A (en) * | 2018-02-27 | 2018-08-07 | 山东禹王生态食业有限公司 | The method of fat solvent removal device and removal grease internal solvent |
-
2009
- 2009-11-26 CN CN2009202584897U patent/CN201567322U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104327946A (en) * | 2014-10-31 | 2015-02-04 | 新疆正企生物科技有限公司 | Purification device and process for crude cotton seed oil produced by leaching process |
| CN108373944A (en) * | 2018-02-27 | 2018-08-07 | 山东禹王生态食业有限公司 | The method of fat solvent removal device and removal grease internal solvent |
| CN108373944B (en) * | 2018-02-27 | 2021-11-19 | 山东禹王生态食业有限公司 | Grease solvent removing device and method for removing solvent in grease |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20100901 Termination date: 20151126 |