CN206553429U - A kind of circulating gas-lifting distillation system that EPA ＆ DHA are extracted from fish oil - Google Patents
A kind of circulating gas-lifting distillation system that EPA ＆ DHA are extracted from fish oil Download PDFInfo
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Abstract
The utility model is related to a kind of circulating gas-lifting distillation system that EPA＆DHA is extracted from fish oil, and the system includes air lift rectifying column, and the tower top of air lift rectifying column is connected with heat exchange tower top；The bottom of towe of air lift rectifying column produces pump by air lift tower reactor and is connected with air lift tower reactor storage tank, and described air lift rectifying column is also connected with feed preheater and nitrogen heater；Stripper overhead is also connected with scrubbing tower, and the tower top of scrubbing tower is connected with blower fan surge tank, and blower fan surge tank is connected by gas compressor with vacuum buffer tank, and vacuum buffer tank is also connected with vavuum pump and heat exchange columns respectively, and heat exchange columns are also connected with nitrogen heater；The bottom of towe of scrubbing tower is connected by washing tower reactor extraction pump with washing tower reactor storage tank, and the bottom of towe of scrubbing tower is also connected by scrubbing tower circulating pump with recirculation cooler, the top connection of recirculation cooler and scrubbing tower.System of the present utility model does not need high vacuum, and disposable purification can improve EPA＆DHA contents to more than 70%.
Description
Technical field
The utility model is related to fish oil purification technique field, and EPA ＆ DHA in fish oil are purified more particularly, to a kind of
System.
Background technology
Fish oil is rich in a series of polyunsaturated fatty acids of ω 3, and its key component is EPA (eicosapentaenoic acid) ＆ DHA (two
Dodecahexaene acid), nutriment necessary to human growth development is not only, and with prevention cardiovascular and cerebrovascular disease, enhancing
Memory, prevents senile dementia, anti-inflammatory, suppression allergic reaction and tumour growth promote a variety of lifes such as baby's retinal development
Manage function.In recent years, polyunsaturated fatty acid is obtained for extensively in many industries such as medicine, food, fine chemistry industry and field
Application, the fish oil derivative product such as EPA ＆ DHA is in supply falls short of demand situation, and countries in the world government is to the food rich in EPA ＆ DHA
Product exploitation is increasingly paid attention to.
At present, EPA ＆ DHA extracting method and process for refining mainly have low-temperature solvent crystallisation, urea clathrate in fish oil
Method, supercritical fluid extraction and molecularly distilled etc..Low-temperature solvent method needs to use substantial amounts of organic solvent, not only there are
Machine dissolvent residual, and substantial amounts of organic solvent need to be reclaimed, separative efficiency is not high without being commonly used.Urea adduct method will be consumed greatly
, there is solvent recovery, problem of environmental pollution in the organic solvent of amount, and be difficult to separate in the close aliphatic acid of double-strand number.It is Chinese special
Sharp file CN105713721A (application numbers：201610161177.9) method for disclosing DHA and EPA in a kind of fish oil concentrated,
Belong to CO2Supercritical fluid extraction；However, supercritical fluid extraction equipment investment is big, it is necessary to condition of high voltage, and it can only extract
Pigment, stink substance and the part free fatty in fish oil are taken out, the purpose of refined fish oil is only served, it is impossible to high-purity
EPA ＆ DHA.Chinese patent document CN103951556A (application numbers：201410192466.6) one kind is disclosed with deep-sea fish
Oil is raw material, the distillation of separation eicosapentaenoic acid (EPA), clupanodonic acid (DPA) and docosahexaenoic acid (DHA)
Technique, belongs to molecularly distilled；Although molecularly distilled can obtain the EPA ＆ DHA of high-purity, however, it is desirable to which high vacuum is set
Standby, multistage distillation, high energy consumption, cost of equipment maintenance is high, and production capacity is small, it is difficult to the need for meeting industrial actual production.
Chinese patent document CN202881231U (application numbers：201220629614.2) disclose a kind of for ethyl ester fish oil
The continous way subcritical reaction device of hydrolysis, including water tank, the reative cell with water inlet and delivery port and with liquid outlet
Liquid reserve tank, provided with can be by the Water Sproading flowed out from liquid outlet to reaction between the liquid outlet of liquid reserve tank and the water inlet of reative cell
The control structure that can control to react room pressure and temperature, condensation evaporation are additionally provided with the loop structure that room is recycled, reative cell
Tank is provided with the recovery structure that can reclaim the ethanol separated from condensation evaporation tank.The reaction unit is primarily adapted for use in subcritical anti-
Answer process, it is impossible to effectively realize EPA ＆ DHA extraction.
The content of the invention
In view of the shortcomings of the prior art, the utility model provides a kind of circulating gas-lifting essence that EPA ＆ DHA are extracted from fish oil
Evaporate system.
The technical solution of the utility model is as follows：
A kind of circulating gas-lifting distillation system that EPA ＆ DHA are extracted from fish oil, the system includes air lift rectifying column, described
The tower top of air lift rectifying column be connected by gas-gas heat exchanger with stripper overhead storage tank, the bottom of stripper overhead storage tank passes through valve
It is connected with stripper overhead return tank, the bottom of stripper overhead return tank is connected by stripping tower reflux pump with air lift rectifying column；
The bottom of towe of described air lift rectifying column produces pump by air lift tower reactor and is connected with air lift tower reactor storage tank, described air lift
Rectifying column is also connected with feed preheater and nitrogen heater；
Described stripper overhead storage tank is also connected with scrubbing tower, and the tower top of described scrubbing tower is connected with blower fan surge tank,
Described blower fan surge tank is connected by gas compressor with vacuum buffer tank, described vacuum buffer tank also respectively with vavuum pump
With gas-gas heat exchanger connection, gas-gas heat exchanger is also connected with nitrogen heater；
The bottom of towe of described scrubbing tower produces pump by washing tower reactor and is connected with washing tower reactor storage tank, described scrubbing tower
Bottom of towe is also connected by scrubbing tower circulating pump with recirculation cooler, the top connection of recirculation cooler and scrubbing tower.
According to the utility model, it is preferred that the tower diameter of described air lift rectifying column be 380mm-500mm, tower height 13-17m,
The number of plates is 3-6 grades.
According to the utility model, it is preferred that described scrubbing tower is plate column, using 3-6 layers of bubble tray.
Circulating gas-lifting distillation system of the present utility model can use inert gas circulating gas-lifting light component, and pass through backflow side
Formula further realizes that component high-purity is separated, and whole process has merged rectifying and air lift principle, utilized component volatilization degree in fish oil
Difference, carry out the process of the vaporization of many second part and partial condensation, while utilizing hot inert gas air lift light component, reduce light group
The partial pressure divided, promotes light component to develop to the vaporization side of balance, the light component content in heavy phase is further reduced.This practicality
Novel inert gas body is recycled in the entire system, disposable supplement, it is not necessary to extra consumption.
Advantage or beneficial effect of the present utility model：
1st, high vacuum is not needed using circulating gas-lifting distillation system of the present utility model, and disposable purification can be by
EPA ＆ DHA contents are improved to more than 70%.
2nd, coordinate the phegma of various concentrations using circulating gas-lifting distillation system of the present utility model, various ratios can be obtained
The EPA ＆ DHA of example；By the use of inert gas as heat-carrying gas, separative efficiency is high, and material heated time is short, and operating condition is gentle, right
Heat-sensitive substance is survivable；Circulated using inert gas, solvent-free recovery problem, no waste water and discarded object are produced, and are solved
Waste water and fixed-end forces problem；Using inert gas as protection gas, fish oil is prevented to be oxidized, peroxide value is almost 0.
3rd, the utility model circulating gas-lifting distillation system is simple in construction, strong operability, and EPA ＆ DHA in fish oil can be achieved
Serialization purification operations, with significant industrialization prospect；With good security, have in health products, the production of medicine
It is widely applied prospect.
Brief description of the drawings
Fig. 1 is the agent structure schematic diagram of circulating gas-lifting distillation system of the present utility model.
Wherein：T101 air lift rectifying columns；T102 scrubbing towers；E101 feed preheaters；E102 nitrogen heaters；E103 gas gas
Heat exchanger；E104 recirculation coolers；V101 stripper overhead storage tanks；V102 stripper overhead return tanks；V103 air lift tower reactor storage tanks；
V104 washs tower reactor storage tank；V105 blower fan surge tanks；V106 vacuum buffer tanks；P101 air lifts tower reactor produces pump；P102 stripping towers
Reflux pump；P103 washing tower reactor extraction pumps；P104 scrubbing tower circulating pumps；P105 gas compressors；P106 vavuum pumps.
Embodiment
The utility model is described further below by specific embodiment and with reference to accompanying drawing, but not limited to this.Implement
Raw materials used in example is convenient source, and device therefor is conventional equipment, wherein, air lift rectifying column T101 is conventional rectification
Tower.
Embodiment 1
As shown in figure 1, a kind of circulating gas-lifting distillation system that EPA ＆ DHA are extracted from fish oil, the system includes air lift essence
Tower T101 is evaporated, described air lift rectifying column T101 tower top is connected by gas-gas heat exchanger E103 with stripper overhead storage tank V101,
Stripper overhead storage tank V101 bottom is connected by valve with stripper overhead return tank V102, stripper overhead return tank V102 bottom
Portion is connected by stripping tower reflux pump P102 with air lift rectifying column T101；
Described air lift rectifying column T101 bottom of towe produces pump P101 and air lift tower reactor storage tank V103 by air lift tower reactor and connected
Connect, described air lift rectifying column T101 is also connected with feed preheater E101 and nitrogen heater E102；
Described stripper overhead storage tank V101 is also connected with scrubbing tower T102, described scrubbing tower T102 tower top and blower fan
Surge tank V105 connections, described blower fan surge tank V105 is connected by gas compressor P105 with vacuum buffer tank V106, institute
The vacuum buffer tank V106 stated is also connected with vavuum pump P106 and gas-gas heat exchanger E103 respectively, gas-gas heat exchanger E103 also with nitrogen
Hot-air heater E102 connections；
Described scrubbing tower T102 bottom of towe is connected by washing tower reactor extraction pump P103 with washing tower reactor storage tank V104, institute
The scrubbing tower T102 stated bottom of towe is also connected by scrubbing tower circulating pump P104 with recirculation cooler E104, recirculation cooler E104
It is connected with scrubbing tower T102 top.
In the present embodiment, air lift rectifying column T101 tower diameters are 400mm, and tower height 15m, the number of plates is 4 grades, and scrubbing tower T102 is
Plate column, using 6 layers of bubble tray.
In embodiment using circulating gas-lifting distillation system extracted from fish oil EPA ＆ DHA technological process it is as follows：
Whole system is vacuumized using vavuum pump P106, vacuum environment is set up, vavuum pump P106 is closed, from blower fan buffering
Tank V105 inflation inlet inflated with nitrogen, nitrogen system is replaced as by whole system, and most system is evacuated to vacuum for 3~5KPa at last,
Gas compressor P105 is opened, now nitrogen opens nitrogen heater E102, nitrogen is preheated in whole system interior circulation, former
Expect fish oil by feed preheater E101 preheating after enter air lift rectifying column T101, hot nitrogen in air lift rectifying column T101 with
Light phase in raw material is discharged from air lift rectifying column T101 tower tops, and heavy phase (EPA ＆ DHA) is produced from air lift rectifying column T101 tower reactors；
The nitrogen of light phase is carry after gas-gas heat exchanger E103 heat exchange, a part of light phase is condensed, into stripping tower
Storage tank V101 is pushed up, subsequently into stripper overhead return tank V102, by stripping tower reflux pump P102 from air lift rectifying column T101 towers
Top is pumped into T101 air lift rectifying columns, further realizes the multistage distillation of component high-purity separation；Another part is not cooled down
Gas phase enter scrubbing tower T102, scrubbing tower T102 be plate column, using 3-6 layers of bubble tray；Scrubbing tower T102 tower bottoms leads to
Scrubbing tower circulating pump P104 is crossed after recirculation cooler E102 coolings, circulation is played in scrubbing tower T102 towers, further by nitrogen
Light phase in gas is trapped, and light phase content is almost 0 in the nitrogen after scrubbing tower T102 washings；
Nitrogen enters blower fan surge tank V105 from scrubbing tower T102 tower tops, enters vacuum by gas compressor P105 compressions
Surge tank V106, then after the hot nitrogen of gas-gas heat exchanger E103 and air lift rectifying column T101 overhead extractions carries out heat exchange,
Further heated into nitrogen heater E102, squeeze into air lift rectifying column T101 interior circulations and use.
Application examples 1：
Air lift rectifying column T101 tower diameters DN400mm, high 15m, 142 DEG C of tower top temperature, 178 DEG C of column bottom temperature；System is taken out very
Sky after nitrogen is circulated through gas compressor P105, is preheating to 250 DEG C, nitrogen flow is to 4KPa by nitrogen heater E102
1500m3/h；
(EPA ＆ DHA contents 24% in raw material, wherein EPA contains 13% to raw material fish oil inlet amount 25L/h, and quality percentage contains
Amount), after feed preheater E101 is preheating to 140 DEG C, fed from air lift rectifying column T101 middle parts, air lift rectifying column T101 towers
Stream is returned in top by stripping tower reflux pump P102, and reflux temperature is 110 DEG C, and phegma flow is that (composition of phegma is 15L/h
The liquid phase collected when not flowed back under the conditions of this, EPA content is less than 2%, weight/mass percentage composition), from air lift rectifying column T101 tower reactors
EPA ＆ DHA mixtures are produced, EPA ＆ DHA contents are up to 70%, and wherein EPA contains 37%, weight/mass percentage composition.
Application examples 2：
Air lift rectifying column T101 tower diameters DN400mm, high 15m；System is evacuated to 4KPa, 142 DEG C of tower top temperature, bottom of towe temperature
178 DEG C of degree, after nitrogen is circulated through gas compressor P105, is preheating to 250 DEG C, nitrogen flow is by nitrogen heater E102
1500m3/h；
Raw material fish oil inlet amount 25L/h (EPA ＆ DHA contents 25%, weight/mass percentage composition in raw material), by raw material preheating
Device E101 is preheating to after 140 DEG C, is fed from air lift rectifying column T101 middle parts, air lift rectifying column T101 tower tops are flowed back by stripping tower
Pump P102 returns stream, and reflux temperature is 110 DEG C, and phegma flow is that (composition of phegma is EPA content about 6%, DHA to 15L/h
Content is 0, weight/mass percentage composition), EPA ＆ DHA mixtures are produced from air lift rectifying column T101 tower reactors, EPA ＆ DHA contents are reachable
73%, wherein EPA contain 48%, weight/mass percentage composition.
Claims (6)
1. a kind of circulating gas-lifting distillation system that EPA＆DHA is extracted from fish oil, it is characterised in that the system includes air lift rectifying
Tower, the tower top of described air lift rectifying column is connected by gas-gas heat exchanger with stripper overhead storage tank, the bottom of stripper overhead storage tank
It is connected by valve with stripper overhead return tank, the bottom of stripper overhead return tank passes through stripping tower reflux pump and air lift rectifying column
Connection；
The bottom of towe of described air lift rectifying column produces pump by air lift tower reactor and is connected with air lift tower reactor storage tank, described air lift rectifying
Tower is also connected with feed preheater and nitrogen heater；
Described stripper overhead storage tank is also connected with scrubbing tower, and the tower top of described scrubbing tower is connected with blower fan surge tank, described
Blower fan surge tank be connected by gas compressor with vacuum buffer tank, described vacuum buffer tank is also gentle with vavuum pump respectively
Gas heat exchanger is connected, and gas-gas heat exchanger is also connected with nitrogen heater；
The bottom of towe of described scrubbing tower produces pump by washing tower reactor and is connected with washing tower reactor storage tank, the bottom of towe of described scrubbing tower
Also it is connected by scrubbing tower circulating pump with recirculation cooler, the top connection of recirculation cooler and scrubbing tower.
2. the circulating gas-lifting distillation system according to claim 1 that EPA＆DHA is extracted from fish oil, it is characterised in that institute
The tower diameter for the air lift rectifying column stated is 380mm-500mm.
3. the circulating gas-lifting distillation system according to claim 1 that EPA＆DHA is extracted from fish oil, it is characterised in that institute
The tower height 13-17m for the air lift rectifying column stated.
4. the circulating gas-lifting distillation system according to claim 1 that EPA＆DHA is extracted from fish oil, it is characterised in that institute
The number of plates for the air lift rectifying column stated is 3-6 grades.
5. the circulating gas-lifting distillation system according to claim 1 that EPA＆DHA is extracted from fish oil, it is characterised in that institute
The scrubbing tower stated is plate column.
6. the circulating gas-lifting distillation system according to claim 5 that EPA＆DHA is extracted from fish oil, it is characterised in that institute
The plate column stated is using 3-6 layers of bubble tray.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720245102.9U CN206553429U (en) | 2017-03-14 | 2017-03-14 | A kind of circulating gas-lifting distillation system that EPA ＆ DHA are extracted from fish oil |
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| CN201720245102.9U CN206553429U (en) | 2017-03-14 | 2017-03-14 | A kind of circulating gas-lifting distillation system that EPA ＆ DHA are extracted from fish oil |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110743184A (en) * | 2019-11-01 | 2020-02-04 | 新疆东方希望新能源有限公司 | Residual removing processing system and method |
| CN114605256A (en) * | 2022-03-14 | 2022-06-10 | 山东禹王制药有限公司 | Extraction method of fish oil intermediate EPA70 |
-
2017
- 2017-03-14 CN CN201720245102.9U patent/CN206553429U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110743184A (en) * | 2019-11-01 | 2020-02-04 | 新疆东方希望新能源有限公司 | Residual removing processing system and method |
| CN110743184B (en) * | 2019-11-01 | 2022-04-19 | 新疆东方希望新能源有限公司 | Residual removing processing system and method |
| CN114605256A (en) * | 2022-03-14 | 2022-06-10 | 山东禹王制药有限公司 | Extraction method of fish oil intermediate EPA70 |
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