CN107287028A - A kind of alcohol extracting taking technique of oil Class material Ultramicro-powder - Google Patents
A kind of alcohol extracting taking technique of oil Class material Ultramicro-powder Download PDFInfo
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- CN107287028A CN107287028A CN201710711831.3A CN201710711831A CN107287028A CN 107287028 A CN107287028 A CN 107287028A CN 201710711831 A CN201710711831 A CN 201710711831A CN 107287028 A CN107287028 A CN 107287028A
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- ceramic membrane
- oil
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- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B1/00—Production of fats or fatty oils from raw materials
- C11B1/10—Production of fats or fatty oils from raw materials by extracting
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B1/00—Production of fats or fatty oils from raw materials
- C11B1/02—Pretreatment
- C11B1/04—Pretreatment of vegetable raw material
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B1/00—Production of fats or fatty oils from raw materials
- C11B1/10—Production of fats or fatty oils from raw materials by extracting
- C11B1/108—Production of fats or fatty oils from raw materials by extracting after-treatment, e.g. of miscellae
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- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Wood Science & Technology (AREA)
- Organic Chemistry (AREA)
- Extraction Or Liquid Replacement (AREA)
Abstract
A kind of alcohol extracting taking technique of oil Class material Ultramicro-powder, belongs to oil plant extractive technique field.It is characterized in that：Comprise the following steps：Oilseed plant class material is crushed and obtains coarse powder material；Will coarse powder material dry after mix with ethanol and carries out that wet-milling is broken that homogenate is made；Extraction in ceramic membrane extraction equipment will be sent into after homogenate heating, and the mixed liquor progress separation of solid and liquid after extraction is reclaimed into ethanol and obtain plant crude protein simultaneously；Extract vacuum distillation obtained by extraction obtains concentrate while reclaiming ethanol, concentrate cooling is layered and is separated into vegetable crude oil and ethanol compound lard, is vegetable oil after vegetable crude oil refining；By-product is obtained after the further separating alcohol solvent of ethanol compound lard.This technique realizes and does not produce contaminative waste material in oil plant cleanly production, production process, alcohol solvent almost can recycling use completely, and oil plant yield improve more than 26.5%.
Description
Technical field
A kind of alcohol extracting taking technique of oil Class material Ultramicro-powder, belongs to oil plant extractive technique field.
Background technology
Existing fat extracting solvent is n-hexane or " No. 6 solvent naphthas " by primary solvent of n-hexane.Because it is to people
The influence of class health and environment, is constantly under suspicion.N-hexane as fat extracting solvent open defect：
1st, security is lacked：N-hexane burning-point is very low（-28℃~-20℃）, explosion limit is wider（1.2%~7.5%）, combustion explosion
Possibility it is very big.When solvent strength reaches 47mg/L ~ 184mg/L in air, meeting naked light can set off an explosion.
2nd, neuron excitotoxicity is acted on：N-hexane has high volatile, height is fat dissolving and has cumulative effect, and a small amount of suction can be right
The upper respiratory tract produces stimulation, and moderate can produce the phenomenons such as nausea, headache, dizziness, eye and larynx stimulation, and intake 50g can be lethal.
Conjunctiva irritation can be caused by being splashed into eye.
In view of the security of n-hexane and hygienic sex chromosome mosaicism, nineteen ninety U.S. Clean Air Act case（Clern Air Act),
It is formal that n-hexane is classified as 189 pollution air harmful substances.EPA（EPA）Propose to limit solvent leaching from 2004
N-hexane amount is discharged by fuel-displaced factory, formulates《Reduce the solvent loss draft standard of pollution surrounding air》.From that time after hundred
Year brilliant leaching-out technique, by serious challenge.Therefore it is always grease work to find a kind of reproducible solvent that substitutes of resource
Journey technical staff institute is deeply concerned.The U.S., Japan, India and Chinese scholar had once made a large amount of ethanol as extraction grease
Experimental study.U.S. New Orleans southern areas research center is proposed the SRRC techniques using ethanol as extraction grease,
And Cotton Seed Oil Extraction pilot scale has been done, but because excessively high etc. reason of cost fails to realize industrialization so far.The new leaching solvent of selection,
Solvent loss is reduced, new extract technology is developed, it has also become one of focus of oil prodution industry technological innovation.
The content of the invention
The technical problem to be solved in the present invention is：Overcoming the deficiencies in the prior art, there is provided a kind of cost is low, consume energy low, nothing
The alcohol extracting taking technique of the oil Class material Ultramicro-powder of pollutant emission.
The technical solution adopted for the present invention to solve the technical problems is：The alcohol extracting work of the oil Class material Ultramicro-powder
Skill, it is characterised in that：Comprise the following steps：
1）Oilseed plant class material is crushed and obtains coarse powder material；
2）Will coarse powder material dry after mix with ethanol and carries out that wet-milling is broken that homogenate is made；
3）It will be extracted in feeding ceramic membrane extraction equipment after homogenate heating, and the mixed liquor after extraction be subjected to separation of solid and liquid recovery
Ethanol obtains plant crude protein simultaneously；
4）Extract vacuum distillation obtained by extraction obtains concentrate while reclaiming ethanol, concentrate cooling is layered and is separated into
Vegetable crude oil and ethanol compound lard, are vegetable oil after vegetable crude oil refining.
It is preferred that, step 3）Described in separation of solid and liquid reclaim ethanol return to step 2）Wet pulverising step reuse.
It is preferred that, step 2）Described in coarse powder material and ethanol mass ratio be 1:2~3.
It is preferred that, step 2）Described in concentration of alcohol be not less than 95%.
It is preferred that, step 4）Described in vacuum distillation reclaim ethanol return to step 3）Ceramic membrane extraction step repeat
Use.
It is preferred that, the fineness of described coarse powder material is 40 ~ 60 mesh.
Ethanol compound lard obtained by when partial material is extracted further can obtain by-product after separating alcohol solvent.It is excellent
Choosing, step 4）Described in the further separating alcohol solvent of ethanol compound lard after obtain by-product, by-product is gossypol, phosphatide
And/or flavones.
It is preferred that, step 3）The temperature being homogenized after described heating is 45 DEG C ~ 60 DEG C.
It is preferred that, step 3）Described in ceramic membrane extraction equipment include extractor, circulating pump and ceramic membrane, extractor
Bottom connected by circulation pipe with the feed end of ceramic membrane, circulating pump is arranged on circulation pipe, the solidliquid mixture of ceramic membrane
Outlet is connected by feed back pipe with the top of extractor, and the mixture export of ceramic membrane is connected by liquid back pipe and extractor top
It is logical.
It is preferred that, described ceramic membrane extraction equipment has the multistage being arranged in series, and the liquid back pipe of ceramic membrane extraction equipment
Connected with the top of the extractor of higher level's ceramic membrane extraction equipment, the extractor of every grade of ceramic membrane extraction equipment is respectively connected with charging
Pipe, the mixture export of the ceramic membrane of every grade of ceramic membrane extraction equipment is respectively connected with drain pipe, and drain pipe is provided with liquid valve, returns
Liquid pipe is provided with back liquid valve.
It is preferred that, the heat exchanger for adjusting solidliquid mixture temperature is connected with described circulation pipe.
Ethanol mixes possibility with grease when the present invention eliminates low amount ratio by specific process sequence and process conditions
The harmful effect caused so that the ethanol of low amount ratio is achieved as the solvent of oil extraction.The low amount ratio of the present invention
Ethanol make it that the security of technique is higher as the realization of the solvent of oil extraction.And ethanol does not have toxic side effect, food is used as
Oil extraction solvent food security is secure.Ethanol source is wide, cost is low, and resource is renewable, environmentally friendly.
Grease has higher solubility in high temperature ethanol, and the solubility in cold ethanol is very low（1% or so）.Profit
This characteristic is used, the present invention is using heating extraction compound lard, and the method that sub-cooled separates out grease obtains crude oil, isolates
Alcohol solvent, because its oil content is very low, can be recycled directly as extractant so as to reducing traditional extract technology just
The expense of hexane evaporation.
Compared with traditional n-hexane solvent, the alcohol solvent that the present invention is realized can also leach the aspergillus flavus in oil plant
The materials such as element, gossypol, phosphatide, more preferably ensure that the edible safety and trophism of oil meal.And the ethanol of the present invention was extracted
Journey is low-temperature extraction, it is to avoid the denaturation of albumen in oil meal, so as to add protein content.It is experimentally confirmed that extracting work with ethanol
The soybean oil meal color and luster that skill is obtained is pure white, eliminates beany flavor, is the very good material of soybean processing protein isolate.
The present invention is also different from the crude oil reparation technology of traditional handicraft：Conventional solvent extract technology by concentration and recovery just oneself
Alkane, obtains crude oil.Crude oil colour is high, and non-oil component is high, has dissolvent residual, impurity is more, and refining loss is big, it is impossible to directly use.
The present invention uses ceramic membrane micro mist extraction process, by the dissolubility difference of grease at different temperatures in ethanol, by low
Temperature condenses ethanol compound lard and separates out crude oil.Crude oil lighter color, free from admixture, and non-oil component is few, only need to simply refine must
To refined oil.
The present invention has obvious advantage than oil meal quality made from traditional handicraft：Conventional solvent extract technology oil meal Residual oil
Rate is high, and color is pale yellow, and content of phospholipid is high, and mutability, beany flavor is dense, and protein content is low.The present invention uses ceramic membrane micro mist
Extraction process, because ethanol has preferable solubility to phosphatide, while Flavonoid substances can be extracted, therefore dregs of beans is pure white, phosphorus
Fat content is low, free from beany flavor, and protein content is high, is adapted to extract soybean protein isolate, while while lecithin is separated, can
To isolate isoflavones.
The present invention prepares grease yield than traditional handicraft and significantly improved：Because Ultramicro-powder can be effectively increased solvent in the present invention
The specific surface area contacted with oil plant, accelerates solute mass transfer velocity, therefore can significantly improve grease yield.Extracted with ceramic membrane differential
The control of cottonseed oil experimental data is taken to be illustrated, cottonseed oil yield has been respectively increased 27.66%, 26.52%, 27.16%.
Compared with prior art, a kind of alcohol extracting taking technique of oil Class material Ultramicro-powder of the invention is had the advantage that
It is：
1st, the alcohol extracting taking technique ethanol of this oil Class material Ultramicro-powder is extracted as extractant combination ceramic membrane extraction equipment
Oil plant, is realized and does not produce contaminative waste material in oil plant cleanly production, production process, and alcohol solvent can almost be reclaimed completely
Recycle, and the yield of oil plant improves more than 26.5%；
2nd, grease has higher solubility in high temperature ethanol, and the solubility in cold ethanol is very low（1% or so）.Utilize
This characteristic, the present invention is using heating extraction compound lard, and the method that sub-cooled separates out grease obtains crude oil, isolates
Alcohol solvent, because its oil content is very low, can directly as extractant recycle so as to reduce traditional extract technology just oneself
The expense of alkane evaporation；
3rd, material and ethanol are mixed into homogenate state with small mass ratio, so as to make material formation flow-like, facilitate material
Conveying and addition；
4th, the heating of homogenate can improve the rate of extraction of active ingredient, and boiling point of the temperature less than ethanol of homogenate, so as to keep away
Exempt from ethanol in extraction process to seethe with excitement；
5th, ceramic membrane extraction equipment realizes the extraction of the ultra micro powder material of oil Class material, farthest improves oil plant
Yield, has saved plant resources, and extract solution separation accuracy reaches 25nm, completely clarification, eliminates other extraction equipments heavy
Extract solution separable programming, is conducive to the processing of subsequent technique, and due to the shear action and material and ceramic membrane of circulating pump
Between fricting shearing, material is crushed, therefore need to only be crushed to the granularity of 100 mesh, i.e. fine powder degree, with regard to that can reach
The effect that Ultramicro-powder is extracted, i.e., in the presence of circulating pump and ceramic membrane, material can be morcelled the mesh of paper 200 ~ 300, by running
" separating twice " function in journey, the problem of ultramicro grinding cost is high, production capacity is small is also readily solved, and reduces crushing cost；
6th, ceramic membrane extraction equipment has the multistage being arranged in series, and realizes continuous extraction, and farthest improving plant has
The yield of composition is imitated, plant resources has been saved, system-wide Automated condtrol and control of product quality can be achieved, be can be achieved single
The combination of branch ceramic-film tube, can also complete the combination of many ceramic-film tubes, and production scale is arbitrarily controlled.Therefore, Ultramicro-powder thing
The ceramic membrane continuous countercurrent extraction technique of material can realize big yield, large-scale production, and small lot and compound medicine can be met again
The continuous production of thing, compact equipment in addition, floor space is small, both can equip independent operating with single group, again can be across group
Connection, is repaired, using very convenient；
7th, because circulating pump has friction between shear action, and ceramic membrane and material to material also to thing when conveying material
Material produces shear action, therefore the temperature of material and extractant can be caused raise, heat exchanger can make material in extractor with
Extractant maintains constant temperature, that is, avoids that temperature is too high to cause solvent to volatilize, and material can be made to extract at a suitable temperature again, so that
Improve rate of extraction；
8th, the process of ethanol is reclaimed in extract vacuum distillation in the present invention, is that progress is micro- using the temperature of extract itself as thermal source
Vacuum distillation is operated, holding -0.02MPa ~ -0.04MPa tiny structure in distillation still.This process utilizes the self heat of extract
Tiny structure distillation is carried out, without extra additional heat again.
Ethanol as solvent of the present invention extracts grease with ceramic membrane micro mist extraction process, can be widely used for soybean, peanut, dish
Seed, cottonseed oil, the extraction of maize germ oil, are also suitable for the small kind functional health such as peony seed oil, sunflower oil, grape-kernel oil
The production of oil.
Brief description of the drawings
Fig. 1 is the process route chart for the alcohol extracting taking technique that the embodiment of the present invention 1 carries out Ultramicro-powder to soybean.
Fig. 2 is the structural representation of plant ultra-micropowder extraction element.
Fig. 3 is the schematic cross-sectional view of shower nozzle.
Fig. 4 is the schematic top plan view of liquid barrier.
Fig. 5 is the schematic perspective view of spoiler.
Fig. 6 is the structural representation of continuous extracting device.
In figure：1st, voltage-stabiliser tube 2, feed pipe 3, condenser 4, inlet valve 5, liquid feed valve 6, feed tube 7, carry
Take tank 8, shower nozzle 801, communicating pipe 802, cone-shaped hood 803, annular slab 804, liquid barrier 805, flow-disturbing platform 9,
Enter flow meters 10, solidliquid mixture delivery pipe 11, solidliquid mixture transfer valve 12, liquid feeding pump 13, discharge nozzle
14th, outlet valve 15, circulation pipe 16, circulating pump 17, heat exchanger 18, circulating valve 19, residue outlet 20, valve of slagging tap
21st, backwash tube 22, mixed liquor transfer valve 23, mixed liquor delivery pipe 24, backwash valve 25, time flow meters
26th, liquid valve 27, drain pipe 28, time liquid valve 29, feed back pipe 30, spoiler 31, ceramic membrane 32, material returning valve
33rd, concentrate delivery pipe 34, liquid back pipe.
Embodiment
Fig. 1 ~ 6 are highly preferred embodiment of the present invention, and 1 ~ 6 the present invention will be further described below in conjunction with the accompanying drawings.
Embodiment 1
As shown in Figure 1：
1）Obtain defilming soybean is broken coarse powder material and cross 40 mesh sieves；
2）By coarse powder material dry after with concentration be 96% ethanol in mass ratio 1：2.4 mixing carry out that wet-milling is broken that homogenate is made；
3）Homogenate is warming up to send into ceramic membrane extraction equipment after 50 DEG C and extracted；
As shown in Figure 2：Ceramic membrane extraction equipment includes extractor 7, circulating pump 16 and ceramic membrane 31, and the bottom of extractor 7 leads to
The feed end that circulation pipe 15 is crossed with ceramic membrane 31 is connected, and circulating pump 16 is arranged on circulation pipe 15, the solid-liquid mixing of ceramic membrane 31
Thing outlet is connected by feed back pipe 29 with the top of extractor 7, and the mixture export of ceramic membrane 31 passes through liquid back pipe 34 and extraction
The top of tank 7 is connected.This plant ultra-micropowder extraction element realizes the extraction of plant ultra-micropowder material, farthest improves plant
The yield of thing active ingredient, has saved plant resources, and extract solution separation accuracy reaches 25nm, completely clarification, eliminates other and carries
The heavy extract solution separable programming of taking equipment, is conducive to the processing of subsequent technique, and due to circulating pump 15 shear action with
And the fricting shearing between material and ceramic membrane 31, material is crushed, therefore need to only be crushed to the granularity of 100 mesh, i.e.,
Fine powder degree, with regard to that can reach the effect that Ultramicro-powder is extracted, i.e., in the presence of circulating pump 16 and ceramic membrane 31, material can be morcelled paper
200 ~ 300 mesh, by " separating twice " function in running, the problem of ultramicro grinding cost is high, production capacity is small also meet sword and
Solution；
The upper end of extractor 7 is connected with feed pipe 2 and feed tube 6, and feed pipe 2 is used into extractor 7 convey material and extraction
The solidliquid mixture of agent, feed tube 6 is used to convey extractant into extractor 7, and feed pipe 2 is provided with inlet valve 4, feed tube 6
It is provided with liquid feed valve 5.Liquid feeding pump 12 is also sequentially provided with along the conveying direction of extractant and enter flow meters 9, feed liquor on feed tube 6
Pump 12 is used to extractant being delivered in extractor 7, enter flow meters 9 be used for measure the extractant that conveys into extractor 7
Amount；
The upper end of extractor 7 is also associated with Voltage stabilizing module, and Voltage stabilizing module is included under voltage-stabiliser tube 1 and condenser 3, voltage-stabiliser tube 1
End is connected with the top of extractor 7, and condenser 3 is arranged on voltage-stabiliser tube 1.Due to circulating pump in extraction process shear action with
And the fricting shearing between material and ceramic membrane 31, the solidliquid mixture of material and extractant can be caused to heat up, and then cause extraction
Agent is taken to evaporate, voltage-stabiliser tube 1 can make the air pressure in extractor 7 remain constant, it is to avoid be counteracted to the cycling extraction of material, cold
Condenser can make extractant steam liquefied, it is to avoid extractant steam is directly discharged in air pollute environment.Voltage-stabiliser tube 1 it is another
End can connect extractant collecting tank, it is preferred that the voltage-stabiliser tube 1 of the upside of extractor 7 is vertically arranged, so as to make after liquefaction
Extractant is back in extractor 7 again, so as to avoid the amount of extractant of measurement from there is error；
The bottom of extractor 7 is connected with solidliquid mixture delivery pipe 10, liquid feeding end and the extractor 7 of solidliquid mixture delivery pipe 10
Bottom connection, the discharge end of solidliquid mixture delivery pipe 10 connects with the liquid feeding end of circulation pipe 15, solidliquid mixture delivery pipe
10 are provided with solidliquid mixture transfer valve 11.The outlet end of solidliquid mixture delivery pipe 10 is also associated with discharge nozzle 13, discharge nozzle
13 are used to that the material submitting extractor 7 completed will to be extracted, and are delivered to specified location, and discharge nozzle 13 is provided with outlet valve 14.Follow
Endless tube 15 is provided with circulating valve 18, so as to pass through the switch of circulating valve 18 and outlet valve 14, the cycling extraction of control material
Or output, it is easy to operate；
Circulation pipe 15 between circulating valve 18 and ceramic membrane 31 is provided with heat exchanger 17, and heat exchanger 17 is used to adjust material and extraction
The temperature of agent, and make the temperature of material and extractant maintain the temperature of optimum extraction, thus improve in material effectively into
The rate of extraction divided.Further, since circulating pump 16 is to the friction between the shear action and material and ceramic membrane 31 of material, meeting
Cause the temperature of the solidliquid mixture of material and extractant persistently overheating in extraction process, so as to have impact on material active ingredient
Extraction；
In the present embodiment, ceramic membrane 31 is provided with two, and the discharge end of a ceramic membrane 31 enters with another ceramic membrane 31
Expect end connection, so that two ceramic membranes 31 are arranged in series, the solidliquid mixture of extractant and material sequentially passes through two ceramic membranes
Flowed back to after 31 by feed back pipe 19 in extractor 7.Two ceramic membranes 31 can improve the speed of extractant separation.Two ceramic membranes 31
Mixture export connected with liquid back pipe 34 so that in mixed-liquor return to extractor 7；
Be provided with mixed liquor delivery pipe 23 between ceramic membrane 31 and liquid back pipe 34, the liquid feeding end of mixed liquor delivery pipe 23 simultaneously with two
The mixture export connection of ceramic membrane 31, and the mixture export of each ceramic membrane 31 is respectively connected with mixed liquor transfer valve 22, mixes
The outlet end for closing liquid delivery pipe 23 is connected with the liquid feeding end of liquid back pipe 34.Mixed liquor delivery pipe 23 is provided with back flow meters 25,
The amount that flow meters 25 are used to measure the mixed liquor of backflow is returned, so as to be engaged with entering flow meters 9, to mixed in extractor 7
Liquid is closed to be monitored in real time.The outlet end of mixed liquor delivery pipe 23 is also associated with drain pipe 27, the one end of drain pipe 27 and mixed liquor
Delivery pipe 23 is connected, and the other end is used to mixed liquor being delivered to specified location.Drain pipe 27 is provided with liquid valve 26, liquid back pipe 34
Liquid valve 28 is provided with back, liquid valve 26 and time liquid valve 28 coordinate, so as to control mixed liquor to send out or send back in extractor 7,
And it is easy to control；
Two ceramic membranes 31 are vertically arranged, and backwash tube 21, backwash tube are respectively connected with the outside of the upper end of two ceramic membranes 31
21 connect with the outside of two ceramic membranes 31 simultaneously, and are each equipped with backwash valve between ceramic membrane 31 and backwash tube 21
24.Residue outlet 19 is connected with the pipeline for connecting two lower ends of ceramic membrane 31, residue outlet 19 is provided with valve 20 of slagging tap, so as to
It is engaged, ceramic membrane 31 is backwashed with backwash tube 21 when ceramic membrane 31 is blocked, and cleaning is convenient.
The liquid feeding end of feed back pipe 29 is connected with the discharge end of ceramic membrane 31, and the discharge end of feed back pipe 29 is stretched into extractor 7,
And the discharge end of feed back pipe 29 is provided with shower nozzle 8, the feed end that shower nozzle 8 deviates solidliquid mixture delivery pipe 10 is set, i.e. shower nozzle 8
Feed end with solidliquid mixture delivery pipe 10 is not coaxial；
As shown in Fig. 3 ~ 4：Shower nozzle 8 includes communicating pipe 801, cone-shaped hood 802 and liquid barrier 804, the upper end of communicating pipe 801 be into
Expect end, lower end is discharge end, and the feed end of communicating pipe 801 is connected with the discharge end of feed back pipe 29.Cone-shaped hood 802 is from top to bottom
The taper that diameter gradually increases, the discharge end of communicating pipe 801 is stretched into cone-shaped hood 802 by top, and with cone-shaped hood 802 is coaxial connects
Connect.Liquid barrier 804 is co-axially located in the cone-shaped hood 802 of the downside of communicating pipe 801, and liquid barrier 804 and the discharging of communicating pipe 801
End is arranged at intervals.Multiple flow-disturbing platforms 805 are interval with around axis, flow-disturbing platform 805 is arc, and flow-disturbing platform on liquid barrier 804
805 one end are arranged on the outer of liquid barrier 804, and the other end is arranged on the side in the center of circle of liquid barrier 804, so that in liquid barrier
Dispersion area is formed on the upside of 804 middle part, facilitates material dispersion, annular is passed through between the discharge end and cone-shaped hood 802 of communicating pipe 801
Plate 803 is closed, it is to avoid material reflux is between communicating pipe 801 and cone-shaped hood 802；
As shown in Figure 5：Flow-disturbing module is provided with extractor 7 on the upside of the feed end of solidliquid mixture delivery pipe 10.Flow-disturbing module
Including vertically disposed two spoilers 30, the width of spoiler 30 is slightly larger than the external diameter of solidliquid mixture delivery pipe 10.Flow-disturbing
Plate 30 is engaged with shower nozzle 8, so as to avoid the solidliquid mixture of extractant and material from forming eddy flow in extractor 7, have impact on
The mixing of extractant and material, and influence material to enter in solidliquid mixture delivery pipe 10；
As shown in Figure 6：Ceramic membrane extraction equipment is provided with multistage, the outlet end of the liquid back pipe 34 of ceramic membrane extraction equipment and higher level
The top connection of the extractor 7 of ceramic membrane extraction equipment, so that extractant can be successively to ceramic membrane extraction equipments at different levels
Homogenate in extractor 7 is extracted.The outlet end of each ceramic membrane extraction equipment drain pipe 27 is all connected with concentrate delivery pipe
33, the mixed liquor that concentrate delivery pipe 33 simultaneously isolates the ceramic membrane 31 of multistage ceramic membrane extraction equipment is sent out.Last
The liquid back pipe 34 of level ceramic membrane extraction equipment is connected with the top of the extractor 7 of first order ceramic membrane extraction equipment, so as to
Ensure that the grease in the mixed liquor of the output of concentrate delivery pipe 33 almost reaches saturation state.Feed back pipe 29 is provided with material returning valve
32, so that the break-make of convenient control feed back；
The series of ceramic membrane extraction equipment is arranged as required to, in the present embodiment, and ceramic membrane extraction equipment is provided with level Four.Often
Sub-feed tube can also be set between the ceramic membrane extraction equipment of adjacent two-stage, and sub-feed tube feed end is mixed with the solid-liquid of ceramic membrane 31
Thing outlet, the discharge end of sub-feed tube is connected with the top of the extractor 7 of next stage ceramic membrane extraction equipment, is set on sub-feed tube
Material distributing valve is put, so as to make material and ethanol form reverse-flow extraction, extraction rate is fast；
Homogenate in Agitation Tank is sequentially added in the extractor 7 of every grade of ceramic membrane extraction equipment by feed pipe 2, and extracted
During to pass through feed pipe 2 be the supplement homogenate of extractor 7 per primary ceramic membrane extraction equipment.It is per one-level by feed tube 6
It is that dress is extracted per primary ceramic membrane to be passed through in the extractor 7 of ceramic membrane extraction equipment in ethanol, and extraction process by feed tube 6
Supplement ethanol in the extractor 7 put., can be quick when some or certain several plant ultra-micropowder extraction elements break down
The connection of pipeline is adjusted, so that crossing the plant ultra-micropowder extraction element broken down continues to complete extraction work, is conveniently set
Standby maintenance, and plant maintenance does not interfere with extraction work；
4）Open the circulation pump 16 carries out extracting operation.When membrane channels of the mixed material high speed by the extraction equipment of ceramic membrane 31,
Mixed liquor after extraction, is separated, and flows to next stage ceramic membrane extraction equipment, mixed material, i.e. solidliquid mixture are flowed back to
Extractor 7.Extract after extraction is sent out by concentrate delivery pipe 33；
As shown in Figure 1：Mixed liquor after extraction is subjected to separation of solid and liquid and reclaims ethanol while obtaining coarse soybean-protein；Extraction gained
Extract vacuum distillation obtain concentrate while reclaim ethanol, concentrate cooling, which is layered, is simultaneously separated into crude oil of soybean and ethanol
Compound lard, is soybean oil after crude oil of soybean refining, the more traditional n-hexane extract technology of soybean oil yield improves 27.66%；
5）Soybean lecithin and isoflavones are obtained after the further separating alcohol solvent of ethanol compound lard.
Embodiment 2
1）Obtain sunflower seeds is broken coarse powder material and cross 50 mesh sieves；
2）By coarse powder material dry after with concentration be 96% ethanol in mass ratio 1：2.2 mixing carry out that wet-milling is broken obtains into homogenate；
3）Homogenate is warming up to send into ceramic membrane extraction equipment after 45 DEG C and extracted, extraction process be the same as Example 1, solvent is solid-liquid
The alcohol solvent of separation and recovery, and the mixed liquor after extraction is subjected to separation of solid and liquid recovery ethanol while obtaining the thick egg of sunflower seeds
In vain；
4）Extract vacuum distillation obtained by extraction obtains concentrate while reclaiming ethanol, concentrate cooling is layered and is separated into
Sunflower seeds crude oil and ethanol compound lard, are sunflower oil, the more traditional n-hexane of sunflower oil yield after the refining of sunflower seeds crude oil
Extract technology improves 27.16%.
Embodiment 3
1）The broken peeling of cottonseed is obtained into coarse powder material and crosses 60 mesh sieves；
2）By coarse powder material dry after with concentration be 95% ethanol in mass ratio 1：2.5 mixing carry out that wet-milling is broken obtains into homogenate；
3）Homogenate is warming up to send into ceramic membrane extraction equipment after 60 DEG C and extracted, extraction process be the same as Example 1, solvent is solid-liquid
The alcohol solvent of separation and recovery, and the mixed liquor after extraction is subjected to separation of solid and liquid recovery ethanol while obtaining cottonseed crude protein；
4）Extract vacuum distillation obtained by extraction obtains concentrate while reclaiming ethanol, concentrate cooling is layered and is separated into
Crude cotton seed oil and ethanol compound lard, are cottonseed oil, the more traditional n-hexane extract technology of cottonseed oil yield after crude cotton seed oil refining
Improve 26.52%；
5）Gossypol is obtained after the further separating alcohol solvent of ethanol compound lard.
The above described is only a preferred embodiment of the present invention, being not the limitation for making other forms to the present invention, appoint
What those skilled in the art changed or be modified as possibly also with the technology contents of the disclosure above equivalent variations etc.
Imitate embodiment.But it is every without departing from technical solution of the present invention content, the technical spirit according to the present invention is to above example institute
Any simple modification, equivalent variations and the remodeling made, still fall within the protection domain of technical solution of the present invention.
Claims (10)
1. a kind of alcohol extracting taking technique of oil Class material Ultramicro-powder, it is characterised in that：Comprise the following steps：
1）Oilseed plant class material is crushed and obtains coarse powder material；
2）Will coarse powder material dry after mix with ethanol and carries out that wet-milling is broken that homogenate is made；
3）It will be extracted in feeding ceramic membrane extraction equipment after homogenate heating, and the mixed liquor after extraction be subjected to separation of solid and liquid recovery
Ethanol obtains plant crude protein simultaneously；
4）Extract vacuum distillation obtained by extraction obtains concentrate while reclaiming ethanol, concentrate cooling is layered and is separated into
Vegetable crude oil and ethanol compound lard, are vegetable oil after vegetable crude oil refining.
2. the alcohol extracting taking technique of oil Class material Ultramicro-powder according to claim 1, it is characterised in that：Step 3）Described in
The ethanol return to step 2 that separation of solid and liquid is reclaimed）Wet pulverising step reuse.
3. the alcohol extracting taking technique of oil Class material Ultramicro-powder according to claim 1 or 2, it is characterised in that：Step 2）In
Described coarse powder material and the mass ratio of ethanol are 1:2~3.
4. the alcohol extracting taking technique of oil Class material Ultramicro-powder according to claim 1, it is characterised in that：Step 4）Described in
Vacuum distillation reclaim ethanol return to step 3）Ceramic membrane extraction step reuse.
5. the alcohol extracting taking technique of oil Class material Ultramicro-powder according to claim 1, it is characterised in that：Described coarse powder material
Fineness be 40 ~ 60 mesh.
6. the alcohol extracting taking technique of oil Class material Ultramicro-powder according to claim 1, it is characterised in that：Step 4）Described in
The further separating alcohol solvent of ethanol compound lard after obtain by-product, by-product is gossypol, phosphatide and/or flavones.
7. the alcohol extracting taking technique of oil Class material Ultramicro-powder according to claim 1, it is characterised in that：Step 3）Described
The temperature being homogenized after heating is 45 DEG C ~ 60 DEG C.
8. the alcohol extracting taking technique of oil Class material Ultramicro-powder according to claim 1, it is characterised in that：Step 3）Described in
Ceramic membrane extraction equipment include extractor（7）, circulating pump（16）And ceramic membrane（31）, extractor（7）Bottom by following
Endless tube（15）With ceramic membrane（31）Feed end connection, circulating pump（16）It is arranged on circulation pipe（15）On, ceramic membrane（31）Consolidate
Liquid mixture outlet passes through feed back pipe（29）With extractor（7）Top connection, ceramic membrane（31）Mixture export by return
Liquid pipe（34）With extractor（7）Top is connected.
9. the alcohol extracting taking technique of oil Class material Ultramicro-powder according to claim 8, it is characterised in that：Described ceramic membrane
Extraction equipment has the multistage being arranged in series, and the liquid back pipe of ceramic membrane extraction equipment（34）With carrying for higher level's ceramic membrane extraction equipment
Take tank（7）Top connection, the extractor of every grade of ceramic membrane extraction equipment（7）It is respectively connected with feed pipe（2）, every grade of ceramic membrane extraction
Take the ceramic membrane of device（31）Mixture export be respectively connected with drain pipe（27）, drain pipe（27）It is provided with liquid valve（26）,
Liquid back pipe（34）It is provided with back liquid valve（28）.
10. the alcohol extracting taking technique of oil Class material Ultramicro-powder according to claim 8, it is characterised in that：Described circulation
Pipe（15）On be connected with heat exchanger for adjusting solidliquid mixture temperature（17）.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108641816A (en) * | 2018-05-09 | 2018-10-12 | 大连理工大学 | A method of extraction rice bran oil |
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Application publication date: 20171024 |