CN206814720U - A kind of continous way supercritical CO 2 refining edible fat production equipment - Google Patents
A kind of continous way supercritical CO 2 refining edible fat production equipment Download PDFInfo
- Publication number
- CN206814720U CN206814720U CN201720525286.4U CN201720525286U CN206814720U CN 206814720 U CN206814720 U CN 206814720U CN 201720525286 U CN201720525286 U CN 201720525286U CN 206814720 U CN206814720 U CN 206814720U
- Authority
- CN
- China
- Prior art keywords
- edible oil
- valve
- carbon dioxide
- tower
- extraction tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Fats And Perfumes (AREA)
- Edible Oils And Fats (AREA)
Abstract
A kind of production equipment of continous way supercritical CO 2 refining edible oil.Mainly solve the problems, such as traditional refining raw food oil process efficiency it is low, it is oxidizable, need three-protection design, have dissolvent residual.Including carbon dioxide storage tank, refrigeration system, CO 2 high pressure pump, crude oil high-pressure pump, extraction tower, distributor, knockout tower, refined edible oil degassing tank, negative pressure pump, crude oil distributor and carbon dioxide distributor are provided with extraction tower, after the carbon dioxide in extraction tower reaches supercriticality, carbon dioxide and crude oil are pumped into extraction tower simultaneously, make two-phase by quickly dissolving, carbon dioxide brings the edible oil of dissolving into knockout tower separation, refined edible oil under pressure-reducing valve discharge and suction function by sucking refined edible oil degassing tank, and undissolved residue is settled down to extraction tower bottom and discharges and suck extraction residue storage tank.The utility model is simple in construction, efficiency high, keeps edible oil original natural component and flavor constant, realizes continuous production.
Description
Technical field
The utility model belongs to chemical mechanical equipment field, and in particular to a kind of continous way supercritical CO 2 refining food
With oily production equipment.
Background technology
Edible oil is cooking dish and fries the primary raw material of food, and qualified edible oil concerns national economy, and its quality is straight
Connect the health for affecting people.Containing many right in the edible vegetable oil and fat without refining treatment obtained through squeezing or lixiviation process
The harmful impurity of human body, such as grease, mixed material dirt powder, cake slag, fiber and other solids are miscellaneous during processing and storage
Matter, moisture content impurity, dissolvent residual etc..The presence of these impurity easily makes color with oil color deepen generation peculiar smell, promotes to become sour, and reduces oil
The quality and use value of fat, are unfavorable for safe storage.If the crude oil obtained through squeezing or lixiviation process is not refined, institute is removed
The impurity contained, toxic action will be produced to human body, influence the health of human body.
As what edible oil and fat were recognized deepens constantly, the aliphatic acid composition of grease have received increasing concern, especially
It is unrighted acid, such as leukotrienes, linoleic acid etc..Linolenic and linoleic is that have special important function to health
Necessary aliphatic acid, in human body can not oneself synthesis, can only be obtained by the intake from the external world, therefore be rich in unsaturated fat
The grease of sour composition has very big Development volue.But the grease of the composition containing unrighted acid is during production and storage
Unsaturated double-bond easily aoxidizes, and causes to go bad, and influences the gentle interest sense of nutritional ingredient of grease.
Supercritical carbon dioxide extraction method is a kind of new separation technology, and the technology is applied to fat-soluble, higher boiling, heat
The extraction of quick property material, has a wide range of applications in the extraction of many products such as biology, medicine, food.Utilize overcritical two
The edible oil quality that carbonoxide is obtained by extraction is higher, the problems such as no solvent residue, it is possible to reduce complicated refining process, saves into
This, saves the energy.The utility model is a kind of continous way supercritical CO 2 refining edible fat production equipment, can be realized super
Critical carbon dioxide extracts edible oil, need to only pass through simple filtering, you can obtain in good taste, quality is high, oxidation stability compared with
Good edible oil, solves the problems such as oxidizable edible oil, refining process complicated and time consumption.
Chinese Patent Application No.：201410118758.5 utility model title：A kind of refining raw food oil technique, it is proposed that
A kind of method for refining raw food oil, it uses traditional depickling, decolouring, the technique of deodorization, and does not possess and have continuity, production efficiency
It is relatively low.
Chinese Patent Application No.：200510054604.5 utility model title：Continuous filtering and refining method for edible oil；
Chinese Patent Application No.：201210375077.8 utility model title：The semicontinuous refinery practice of edible oil；
A kind of equipment and method with continuous production ability are proposed, but it still uses depickling, decolouring, taken off
Smelly traditional handicraft, easily leaves chemical residual, influences health, and is easily destroyed the unrighted acid in grease, makes
Reduced into nutritive value.
Chinese Patent Application No.：201420454258.4 utility model title：A kind of overcritical titanium dioxide of intensified by ultrasonic wave
Carbon extracts the device systems of peony seed oil；Which employs CO 2 extraction technology, but it is the extraction oil from plant powder
Fat, and it does not possess continuity, operating efficiency is relatively low.
Utility model content
In place of the purpose of this utility model is to overcome above-mentioned deficiency, there is provided a kind of simple in construction, speed is fast, and the cycle is short,
Efficiency high, low energy consumption is easy to operate, no waste discharge, does not endanger body, and edible oil original natural component and flavor can be kept constant,
Quantity-produced supercritical CO 2 refining edible fat production equipment can be achieved.
In order to achieve the above object, the utility model adopts the technical scheme that：A kind of continous way supercritical carbon dioxide
Refined edible oil production equipment, including carbon dioxide storage tank, refrigeration system, CO 2 high pressure pump, crude oil high-pressure pump, titanium dioxide
Carbon preheater, crude oil preheater, extraction tower, distributor, knockout tower, refined edible oil degassing tank, negative pressure pump, described titanium dioxide
Carbon storage tank is by pipeline through carbon dioxide supply valve, gas-liquid separator, refrigeration system, liquid CO 2 storage tank, carbon dioxide
High-pressure pump and carbon dioxide preheater are connected after being sequentially connected in series with extraction tower bottom left import, and crude oil storage tank is by pipeline through hair
Crude oil import is connected on the left of oily high-pressure pump, crude oil preheater and extraction tower upper end, in extraction tower upper end be provided with crude oil distributor with
Crude oil import is connected on the left of extraction tower upper end, and lower end is provided with carbon dioxide distributor and on the left of the end of extraction tower lower end two in extraction tower
Carbonoxide import is connected, and extraction tower upper end right-side outlet is by pipeline through pressure regulator valve, dioxide solution preheater, carbon dioxide
Solution stop valve is connected with end entrance on knockout tower, extraction tower bottom be provided with extraction residue discharge pressure-reducing valve, by pipeline with
Extract residue storage tank top left hand import connection, extraction residue storage tank top by pipeline through negative pressure valve C connection negative pressure pumps,
Atmospheric valve E is also connected with by the pipeline with pressure gauge, extraction tower outer wall is provided with extraction tower preheater, and knockout tower outer wall is set
There is knockout tower preheater, knockout tower upper end right-side outlet connects gas-liquid separation by pipeline through carbon dioxide return valve, check-valves
Device and carbon dioxide storage tank, separation tower bottom are provided with refined edible oil discharge pressure-reducing valve by pipeline through refined edible oil cut-off valve
A and refined edible oil cut-off valve B pushes up with import on the right side of refined edible oil degassing tank A tops and refined edible oil degassing tank B respectively
The import connection of end left side, refined edible oil degassing tank A and refined edible oil degassing tank B tops by pipeline respectively through negative pressure valve with
Negative pressure valve connects negative pressure pump, is also connected to atmospheric valve C and atmospheric valve D, refined edible oil by the pipeline with pressure gauge
Degassing tank A is respectively equipped with refined edible oil dump valve A and refined edible oil dump valve B with refined edible oil degassing tank B bottoms.
Further, the blade diameter length ratio of described extraction tower designs according to edible oil component and polarity, and diameter is in 50mm-
1000mm, highly in 1000mm-10000mm, material is stainless steel.
Further, the material of the crude oil distributor in described extraction tower and carbon dioxide distributor is by including metal
Material is made, and shape and structure design can be fountain, sieve mesh type, overflow-type, atomizing, material filling type.
Further, the extraction tower preheater of described extraction tower, to be provided with knockout tower preheater, crude oil on knockout tower pre-
Hot device, carbon dioxide preheater, the mode of heating of dioxide solution preheater, may be designed as interlayer heating water bath, ribbon heater
Heating, carbon fiber heating, electromagnetic induction heating.
Further, the blade diameter length ratio of described knockout tower designs according to edible oil component and polarity, and diameter is in 50mm-
1000mm, highly in 1000mm-10000mm, material is stainless steel.
Further, described knockout tower may be designed at least two in the entire system.
Further, the changeable operation operations of described refined edible oil degassing tank A and refined edible oil degassing tank B.
Further, described extraction residue discharge pressure-reducing valve and refined edible oil discharge pressure-reducing valve are stainless steel
Matter, ceramic material, graphite material.
The utility model has the advantages that：By using the technical solution of the utility model
1st, realize that edible oil and supercritical carbon dioxide continuous liquid-liquid extract, improve utilization rate of equipment and installations.
2nd, edible oil original natural component, flavor and mouthfeel can be kept constant
3rd, acid number is less than 0.6 after refining, and peroxide value is less than 0.2.
4th, temperature is low, speed is fast, efficiency high, and refined oil recovery rate is up to more than 95%.
5th, no solvent residue, it is free from environmental pollution, do not endanger body.
6th, low energy consumption, operating cost is reduced.
7th, extraction tower internal upper part is provided with edible oil distributor, edible oil is uniformly distributed from top to down, bottom in extraction tower
Provided with carbon dioxide distributor, make carbon dioxide to it is lower and on be uniformly distributed, so as to increase two-phase each specific surface area, shorten extraction
The time is taken, increases production capacity.
8th, extraction tower and separation tower bottom are designed with depressurizing draining valve, can control oil drain quantity to reduce the passage of carbon dioxide,
Carbon dioxide loss rate is 5%.
9th, refined oil degassing tank deviates from peculiar smell in carbon dioxide and edible oil in the presence of negative pressure.
10th, it is simple in construction, it is easy to operate, labor intensity is reduced, only needs 1 people operation.
Brief description of the drawings：
Fig. 1 is a kind of continous way supercritical CO 2 refining edible fat production equipment schematic diagram of the utility model.
1, carbon dioxide storage tank 2, carbon dioxide supply valve 3, gas-liquid separator 4, refrigeration system 5, liquid in figure
Body carbon dioxide storage tank 6, crude oil storage tank 7, crude oil high-pressure pump 8, CO 2 high pressure pump 9, crude oil preheater 10,
Carbon dioxide preheater 11, carbon dioxide stop valve 12, crude oil stop valve 13, crude oil distributor 14, extraction tower
15th, extraction tower preheater 16, carbon dioxide distributor 17, extraction residue discharge pressure-reducing valve 18, atmospheric valve A 19,
Pressure regulator valve 20, dioxide solution preheater 21, dioxide solution stop valve 22, knockout tower 23, refined edible
Oil discharge pressure-reducing valve 24, carbon dioxide return valve 25, atmospheric valve B 26, knockout tower preheater 27, atmospheric valve C 28,
Negative pressure valve A 29, refined edible oil degassing tank A 30, refined edible oil dump valve A 31, refined edible oil cut-off valve A
32nd, refined edible oil cut-off valve B 33, negative pressure valve B 34, refined edible oil degassing tank B 35, refined edible oil dump valve B
36th, atmospheric valve D 37, extraction residue storage tank 38, extraction residue dump valve 39, atmospheric valve E 40, negative pressure valve C
41st, negative pressure pump 42, check-valves.
Embodiment
The utility model is described further below in conjunction with the accompanying drawings.
A kind of continous way supercritical CO 2 refining edible fat production equipment as shown in Figure 1, including carbon dioxide storage
Tank, refrigeration system, CO 2 high pressure pump, crude oil high-pressure pump, carbon dioxide preheater, crude oil preheater, extraction tower, distribution
Device, knockout tower, refined edible oil degassing tank, negative pressure pump, described carbon dioxide storage tank 1 is by pipeline through carbon dioxide supply valve
2, gas-liquid separator 3, refrigeration system 4, liquid CO 2 storage tank 5, CO 2 high pressure pump 8 and carbon dioxide preheater 10 according to
It is connected after secondary concatenation with the bottom left import of extraction tower 14, crude oil storage tank 6 is by pipeline through crude oil high-pressure pump 7, crude oil preheater 9
It is connected with crude oil import on the left of the upper end of extraction tower 14, it is left with the upper end of extraction tower 14 to be provided with crude oil distributor 13 for upper end in extraction tower 14
Side crude oil import is connected, and lower end is provided with carbon dioxide distributor 16 and carbon dioxide on the left of the lower end end of extraction tower 14 in extraction tower 14
Import is connected, and the upper end right-side outlet of extraction tower 14 is by pipeline through pressure regulator valve 19, dioxide solution preheater 20, carbon dioxide
Solution stop valve 21 is connected with end entrance on knockout tower 22, and the bottom of extraction tower 14 is provided with extraction residue discharge pressure-reducing valve 17, leads to
Piping is connected with the extraction top left hand import of residue storage tank 37, and extraction residue storage tank top is by pipeline through negative pressure valve
C40 connections negative pressure pump 41, is also connected with atmospheric valve E39 by the pipeline with pressure gauge, and the outer wall of extraction tower 14 is provided with extraction tower
Preheater 15；
The described outer wall of knockout tower 22 is provided with knockout tower preheater 26, and the upper end right-side outlet of knockout tower 22 is passed through by pipeline
Carbon dioxide return valve 24, check-valves 42 connect gas-liquid separator 3 and carbon dioxide storage tank 1, and the bottom of knockout tower 22 is provided with refined
Edible oil discharge pressure-reducing valve 23 by pipeline through refined edible oil cut-off valve A31 and refined edible oil cut-off valve B32 respectively with essence
Import connects with refined edible oil degassing tank B34 top left hand imports on the right side of edible oil degassing tank A29 tops processed, refined edible oil
Degassing tank A29 is connected negative pressure pump through negative pressure valve 28 with negative pressure valve 33 respectively with refined edible oil degassing tank B34 tops by pipeline
41, atmospheric valve C27 and atmospheric valve D36 are also connected to by the pipeline with pressure gauge, refined edible oil degassing tank A29 with
Refined edible oil degassing tank B34 bottoms are respectively equipped with refined edible oil dump valve A30 and refined edible oil dump valve B35.
As one embodiment of the present utility model, the blade diameter length ratio of described extraction tower 14 is according to edible oil component and polarity
Design, diameter is in 50mm- 1000mm, and highly in 1000mm-10000mm, material is stainless steel.
As one embodiment of the present utility model, crude oil distributor 13 and carbon dioxide point in described extraction tower 14
The material of cloth device 16 is made up of the material including metal, shape and structure design can be fountain, sieve mesh type, overflow-type, atomizing,
Material filling type.
As one embodiment of the present utility model, on the extraction tower preheater 15 of described extraction tower 14, knockout tower 22
It is provided with the heating of knockout tower preheater 26, crude oil preheater 9, carbon dioxide preheater 10, dioxide solution preheater 20
Mode, it may be designed as interlayer heating water bath, ribbon heater heating, carbon fiber heating, electromagnetic induction heating.
As one embodiment of the present utility model, the blade diameter length ratio of described knockout tower 22 is according to edible oil component and polarity
Design, diameter is in 50mm- 1000mm, and highly in 1000mm-10000mm, material is stainless steel.
As one embodiment of the present utility model, described knockout tower 22 may be designed at least two in the entire system
It is individual.
As one embodiment of the present utility model, described refined edible oil degassing tank A29 and refined edible oil degassing
The changeable operation operations of tank B34.
As one embodiment of the present utility model, described extraction residue discharge pressure-reducing valve 17 and refined edible oil row
It is stainless steel to go out pressure-reducing valve, ceramic material, graphite material.
Specifically, when in use, it is first shut off crude oil stop valve 12, dioxide solution stop valve and extraction residue row
Go out pressure-reducing valve 17, open carbon dioxide supply valve 2, carbon dioxide is flowed through gas-liquid separator 3, refrigeration system 4, carbon dioxide storage
Tank 5, CO 2 high pressure pump 8, carbon dioxide preheater 10, carbon dioxide stop valve 11 enter in extraction tower 14, open simultaneously
Atmospheric valve A18, the air in extraction tower 14 is excluded, it is white gas that observation atmospheric valve A18, which comes out, it was demonstrated that in extraction tower 14
Air has emptied, and is then shut off atmospheric valve A18, opens dioxide solution stop valve 21, makes carbon dioxide pre- through carbon dioxide
Hot device 20 enters in knockout tower 22, while opens atmospheric valve 25, and the air in knockout tower 22 is excluded, and observation atmospheric valve B25 goes out
Come for white gas, it was demonstrated that the air in knockout tower 22 has emptied, and is then shut off atmospheric valve B25, opens carbon dioxide return valve
24, carbon dioxide is back to through check-valves 42 in gas-liquid separator 3, carbon dioxide is full of whole system, system balancing pressure
Power is in 4.5-5Mpa.When the temperature of extraction tower 14 reaches design temperature（Design temperature scope is 35 DEG C -60 DEG C）, the temperature of knockout tower 22
Reach design temperature（Design temperature scope is 45 DEG C -80 DEG C）, when the temperature of refrigeration system 4 reaches less than 5 DEG C（Carbon dioxide liquid
Change）, dioxide solution stop valve 21 is closed, CO 2 high pressure pump 8 is opened, pressure in extraction tower 14 is reached design pressure
（It is 10-40MPa to design extraction tower pressure limit）Afterwards, dioxide solution stop valve 21 is opened, pressure regulator valve 19 is adjusted, makes extraction
The stable dynamic operation in the case where setting pressure of the pressure carbon dioxide in tower is taken, and controls carbon dioxide flow in setting range（If
Constant flow is typically in 0.1 M3-10M3/h）, regulation of carbon dioxide return valve, make the control of separation tower pressure interior force in 6-8Mpa scopes.
After all are stable, crude oil high-pressure pump 7 is opened, makes crude oil by pipeline through crude oil preheater 9, crude oil stop valve 12 and crude oil point
Cloth device 13 enters in extraction tower 14, and crude oil is uniformly distributed by crude oil distributor 13 from top to down, with passing through carbon dioxide distributor
16 cross to lower and upper equally distributed carbon dioxide, and this process increases two-phase each specific surface area each other, and realization is quickly dissolved each other,
Carbon dioxide brings the edible oil of dissolving in knockout tower 22 into, and due to changing pressure and temperature condition, carbon dioxide gasification is through two
The reflux cycle of carbonoxide return valve 24 is utilized, and separated edible oil is settled down in bottom of towe, opens the He of refined edible oil cut-off valve 31
Negative pressure valve 28, atmospheric valve 27 is closed, by controlling refined edible oil oil extraction pressure-reducing valve 23 refined edible oil is slowly discharged, and
Sucked under suction function in refined edible oil degassing tank A29, while the carbon dioxide in refined edible oil and peculiar smell are removed.When
After refined edible oil degassing tank A29 is filled, negative pressure valve 33 is opened, closes atmospheric valve 36, opens refined edible oil cut-off valve B32,
Make in refined edible oil suction refined edible oil degassing tank B34（Switchover operation operates）.Negative pressure valve 28 is closed, opens atmospheric valve
27, after refined edible oil degassing tank A29 is vented, open the refined edible oil dump valve of refined edible oil degassing tank A29 bottoms
A30, both obtain refined edible oil product.After refined edible oil degassing tank B34 is filled, negative pressure valve A28 is opened, closes atmospheric valve
C27, refined edible oil cut-off valve A31 is opened, made in refined edible oil suction refined edible oil degassing tank A29（Switchover operation is grasped
Make）.Negative pressure valve 33 is closed, opens atmospheric valve D36, after refined edible oil degassing tank B34 is vented, opens refined edible oil degassing
The refined edible oil dump valve B35 of tank B34 bottoms, both obtain refined edible oil product.And undissolved extraction residue is settled down to
The bottom of extraction tower 14, extraction residue is slowly discharged by extracting residue oil extraction pressure-reducing valve 17, and inhaled under suction function
Enter to extract in residue storage tank 37, open the extraction residue dump valve 38 of the bottom of extraction residue storage tank 37, must both extract surplus
Excess byproduct, the utility model can realize 24 hours continuous productions, and refined edible oil product yield is more than 95%.
Although embodiment of the present utility model has been shown and described above, it is to be understood that above-described embodiment is
Exemplary, it is impossible to it is interpreted as not departing from the utility model to limitation of the present utility model, one of ordinary skill in the art
Principle and objective in the case of above-described embodiment can be changed in the scope of the utility model, change, replace and
Modification.
Claims (6)
1. a kind of continous way supercritical CO 2 refining edible fat production equipment, including carbon dioxide storage tank, refrigeration system, two
Carbonoxide high-pressure pump, crude oil high-pressure pump, carbon dioxide preheater, crude oil preheater, extraction tower, distributor, knockout tower, refine food
With oily degassing tank, negative pressure pump, it is characterised in that：Described carbon dioxide storage tank（1）By pipeline through carbon dioxide supply valve
（2）, gas-liquid separator（3）, refrigeration system（4）, liquid CO 2 storage tank（5）, CO 2 high pressure pump（8）And carbon dioxide
Preheater（10）It is sequentially connected in series rear and extraction tower（14）Bottom left import is connected, crude oil storage tank（6）By pipeline through crude oil height
Press pump（7）, crude oil preheater（9）With extraction tower（14）Crude oil import is connected on the left of upper end, extraction tower（14）Interior upper end is provided with hair
Oily distributor（13）With extraction tower（14）Crude oil import is connected on the left of upper end, extraction tower（14）Interior lower end is distributed provided with carbon dioxide
Device（16）With extraction tower（14）Carbon dioxide inlet is connected on the left of the end of lower end, extraction tower（14）Upper end right-side outlet is passed through by pipeline
Pressure regulator valve（19）, dioxide solution preheater（20）, dioxide solution stop valve（21）With knockout tower（22）Upper end entrance
It is connected, extraction tower（14）Bottom is provided with extraction residue discharge pressure-reducing valve（17）, pass through pipeline and extraction residue storage tank（37）
Top left hand import connects, and extraction residue storage tank top is by pipeline through negative pressure valve C（40）Connect negative pressure pump（41）, also pass through
Pipeline with pressure gauge is connected with atmospheric valve E（39）, extraction tower（14）Outer wall is provided with extraction tower preheater（15）, knockout tower
（22）Outer wall is provided with knockout tower preheater（26）, knockout tower（22）Upper end right-side outlet is by pipeline through carbon dioxide return valve
（24）, check-valves（42）Connect gas-liquid separator（3）And carbon dioxide storage tank（1）, knockout tower（22）Bottom is provided with refined edible
Oil discharge pressure-reducing valve（23）By pipeline through refined edible oil cut-off valve A（31）And refined edible oil cut-off valve B（32）Respectively with
Refined edible oil degassing tank A（29）Import and refined edible oil degassing tank B on the right side of top（34）Top left hand import connects, and refines
Edible oil degassing tank A（29）With refined edible oil degassing tank B（34）Top is by pipeline respectively through negative pressure valve（28）With negative pressure valve
（33）Connect negative pressure pump（41）, atmospheric valve C is also connected to by the pipeline with pressure gauge（27）And atmospheric valve D（36）,
Refined edible oil degassing tank A（29）With refined edible oil degassing tank B（34）Bottom is respectively equipped with refined edible oil dump valve A（30）
And refined edible oil dump valve B（35）.
2. a kind of continous way supercritical CO 2 refining edible fat production equipment according to claim 1, its feature exist
In：Described extraction tower（14）Blade diameter length ratio designed according to edible oil component and polarity, diameter is in 50mm- 1000mm, height
In 1000mm-10000mm, material is stainless steel.
3. a kind of continous way supercritical CO 2 refining edible fat production equipment according to claim 1, its feature exist
In：Described extraction tower（14）Interior crude oil distributor（13）With carbon dioxide distributor（16）Material by the material including metal
Material is made, and shape and structure design can be fountain, sieve mesh type, overflow-type, atomizing, material filling type.
4. a kind of continous way supercritical CO 2 refining edible fat production equipment according to claim 1, its feature exist
In described knockout tower（22）Blade diameter length ratio designed according to edible oil component and polarity, diameter highly exists in 50mm- 1000mm
1000mm-10000mm, material are stainless steel.
5. a kind of continous way supercritical CO 2 refining edible fat production equipment according to claim 1, its feature exist
In：Described knockout tower（22）At least two are may be designed in the entire system.
6. a kind of continous way supercritical CO 2 refining edible fat production equipment according to claim 1, its feature exist
In：Described extraction residue discharge pressure-reducing valve（17）With refined edible oil discharge pressure-reducing valve（23）For stainless steel, ceramics
Material, graphite material.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720525286.4U CN206814720U (en) | 2017-05-12 | 2017-05-12 | A kind of continous way supercritical CO 2 refining edible fat production equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720525286.4U CN206814720U (en) | 2017-05-12 | 2017-05-12 | A kind of continous way supercritical CO 2 refining edible fat production equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206814720U true CN206814720U (en) | 2017-12-29 |
Family
ID=60754343
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201720525286.4U Expired - Fee Related CN206814720U (en) | 2017-05-12 | 2017-05-12 | A kind of continous way supercritical CO 2 refining edible fat production equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206814720U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107057849A (en) * | 2017-05-12 | 2017-08-18 | 祖柏实 | A kind of continous way supercritical CO 2 refining edible fat production equipment |
-
2017
- 2017-05-12 CN CN201720525286.4U patent/CN206814720U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107057849A (en) * | 2017-05-12 | 2017-08-18 | 祖柏实 | A kind of continous way supercritical CO 2 refining edible fat production equipment |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103519260B (en) | Production technology of red date concentrated clear juice | |
| CN103320220B (en) | Method for distilling and refining high-grade oil by rice bran oil molecules | |
| CN204848801U (en) | Airtight vacuum melting production facility of animal oil | |
| CN109777607B (en) | Method for purifying DHA (docosahexaenoic acid) crude oil | |
| CN103756844B (en) | Functional compound berry wine and production method thereof | |
| CN101554211A (en) | Technique and industrial device for refining rice by supercritical polybasic fluid | |
| CN102295983A (en) | Production method for comprehensive utilization of microalgae | |
| CN102796610A (en) | Production technology for extracting eucommia oil and eucommia protein from eucommia kernels | |
| CN108998196A (en) | A kind of extracting method of microalgae oil DHA | |
| CN105713716A (en) | Method for extracting sea buckthorn fruit oil in grading mode through combination of aqueous enzymatic method and ultrasonic assistance | |
| CN206814720U (en) | A kind of continous way supercritical CO 2 refining edible fat production equipment | |
| CN108676623A (en) | A kind of essential oil extraction device | |
| CN102583855A (en) | Oil-water separation process of pulpifying centrifugal treatment system | |
| CN103911208B (en) | A kind of heterophytic chlorella grease extraction | |
| CN107557140A (en) | The preparation method of Semen Coicis oil extracted from rice husks | |
| CN205653423U (en) | Vegetable oil integration refining equipment | |
| CN109651485A (en) | A kind of extraction of grape pip protein and purification process | |
| CN101748038B (en) | Method for percolating and aging white spirit | |
| CN204737937U (en) | Functional vegetable oil extraction element has | |
| CN107057849A (en) | A kind of continous way supercritical CO 2 refining edible fat production equipment | |
| CN103361172A (en) | Method for refining olive oil | |
| CN103875824A (en) | Preparation method for walnut oil | |
| CN110669581A (en) | Extraction method of microalgae total lipid and microalgae protein meal | |
| CN104938652A (en) | Preparation method of blended edible oil of peony seed oil and walnut oil | |
| CN207672021U (en) | A kind of essential oil extraction device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20171229 |