CN1307093A - Method for extracting raw corn oil from distillers' grains - Google Patents
Method for extracting raw corn oil from distillers' grains Download PDFInfo
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- CN1307093A CN1307093A CN00101787A CN00101787A CN1307093A CN 1307093 A CN1307093 A CN 1307093A CN 00101787 A CN00101787 A CN 00101787A CN 00101787 A CN00101787 A CN 00101787A CN 1307093 A CN1307093 A CN 1307093A
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- oil
- vinasse
- corn oil
- raw corn
- extracting raw
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/74—Recovery of fats, fatty oils, fatty acids or other fatty substances, e.g. lanolin or waxes
Abstract
Through the steps of centrifugal separation, evaporation and drying, pelletizing, stoving and preheating, leaching, evaporation, stripping, alkali refining and water washing, settling, dewatering, filtering, etc. raw corn oil is extracted from distillers' grains. The method is suitable for use especially in continuous corn alcohol producing enterprise.
Description
The invention belongs to chemical field, relate to the byproduct of making alcohol and reclaim.
Existing is raw material manufacturing by product---the vinasse that alcohol produced with corn, is regarded as waste usually, or is used as the feed of making domestic animal.Contain a large amount of raw corn oils in the vinasse and can not get recycling, cause the waste of resource.
The objective of the invention is to, provide a kind of from make the by product that alcohol produced with corn---extract the method for raw corn oil the vinasse, its method advanced person, cost is low, and it is fast to produce effects, and profit is big, is specially adapted to corn and brews alcoholic beverages in the enterprise that smart serialization produces.
The objective of the invention is to realize by following technical scheme:
A kind of method of extracting raw corn oil from vinasse is characterized in that it comprises that successively the following technology step is poly-: heat, leaching, evaporation, stripping, alkali refining washing, sedimentation, dehydration, filtration are given in vinasse centrifugation, evaporation drying, granulation, oven dry.
The particle of granulation is 8-10mm.
Extraction temperature is 50-55 ℃.
Stripping mixing oil temperature out is 110-115 ℃.
The solvent oil that evaporate, stripping comes out and the solvent oil reuse of mixing steam after condensation divides water of water.
The advantage applies of extracting the method for raw corn oil from vinasse of the present invention exists:
1, the technical process advanced person of present method, technological equipment investment is lower, and it is fast to produce effects;
2, owing to extract raw corn oil from vinasse, raw materials cost is low, and profit is big, makes resource fully obtain utilization;
3, present method is specially adapted to corn and brews alcoholic beverages in the enterprise that smart serialization produces.
Embodiment below in conjunction with accompanying drawing is described further the method for extracting raw corn oil from vinasse of the present invention.
Fig. 1 is a process flow sheet of the present invention.
Fig. 2 is a processing unit schema of the present invention.
With reference to Fig. 1, the method of extracting raw corn oil from vinasse of the present invention is characterized in that it comprises following processing step successively: vinasse centrifugation, evaporation drying, granulation, oven dry are given heat, leaching, leaching miscella evaporation, stripping, alkali refining washing, sedimentation, dewatered, are filtered into the finished product crude oil; The wet dregs of rice after the leaching steam and take off, are cooled to the full price distiller's dried grain, can be used as the feed of making domestic animal; The solvent oil that evaporate, steaming is taken off, stripping comes out and the solvent oil reuse of mixing steam after condensation divides water of water.
With reference to Fig. 2, with the by product of preparing alcohol---vinasse are sent into separating centrifuge 1 and are separated, and the processing parameter of separating centrifuge 1 is: service temperature≤100 ℃, separating machine flow 26-28m
3/ h, separating machine rotor speed 3600rpm, wet vinasse dry matter content is 28-32%, the wet vinasse of discharging after separating are delivered to and are carried out drying in the drying machine 2, the processing parameter of drying machine 2 is: temperature 78-92 ℃, vapor pressure 0.55-0.65MPa, 8 rev/mins of rotating cylinder revolutions, isolated clear liquid is by the clear liquid tundish reuse in the potential difference inflow wine producing process.Wet vinasse become vinasse dry powder after evaporation drying, vinasse dry powder is added an amount of steam and the suitable damping of process water, then; enter tablets press 3; tablets press 3 processing parameters are: flooding quantity 50kg/h, throttle flow 320kg/h, service temperature≤100 ℃; vinasse particle diameter after the granulation is 8-10mm; contain moisture≤12%, give heat through plate dryer 4 oven dry, plate dryer 4 processing parameters are: temperature out≤60 ℃; indirect steam pressure is 0.4MPa, outlet moisture content about 10%.Drying is given the vinasse particulate material after the heat, sends into flat-turn leacher 6 by scraper conveyor 5 through the sealing auger, places No. 6 solvent oils in the leacher 6, and solvent oil is to contain the commercially available Chemicals that normal hexane is a major ingredient.In this and solvent oil counter current contact, with abundant extraction grease wherein.Leacher 6 rotating speeds be 100-105 minute/change, extraction temperature is 50-55 ℃, leacher running period is 90-120 minute, solvent oil and material ratio are 1: 0.8-1.
Leach the wet dregs of rice and send into evapo-separated machine 7 processing through the sealing auger by scraper conveyor 22, the mode precipitation that evapo-separated machine 7 adopts open steam to combine with indirect steam, with residual molten the reducing to below the 700ppm of the dregs of rice, go out 105-110 ℃ of dregs of rice temperature, after being cooled off, the dregs of rice become full price distiller's dried grain warehouse-in in cold dregs of rice machine 8.
Leach mixing oil after the tent strainer of leacher 6 filters, enter single vaporization device 10, the processing parameter of single vaporization device 10 is: 60-65 ℃ of mixing oil inlet temperature, 80-85 ℃ of mixing oil temperature out, mixing oil exit concentration 60-65%, indirect steam pressure 0.2-0.3MPa, enter second evaporator 11, the processing parameter of second evaporator 11 is: 80-85 ℃ of mixing oil inlet temperature, 95-100 ℃ of mixing oil temperature out, mixing oil exit concentration 90-95%, indirect steam pressure is 0.3-0.4MPa, and mixing oil enters disk stripping column 12, and the processing parameter of stripping tower 12 is: 90-100 ℃ of mixing oil inlet temperature, 110-115 ℃ of mixing oil temperature out, mixing oil inlet concentration 90-95%, total volatile matter is no more than 0.2%, indirect steam pressure 0.4MPa in the leaching crude oil, tower body is 0.05MPa on the open steam pressure, and following tower body is 0.1MPa.
From leacher 6, the solvent oil that vaporizer 10,11 comes out and the mixing steam of water are introduced condenser 9 respectively, enter comprehensive solvent branch water cycle storehouse 13 after the condensation, solvent oil part reuse wherein.
13 waste water of discharging are delivered to water seal tank 21 and are handled from comprehensive solvent branch water cycle storehouse.
Coarse wool oil behind stripping tower 12 strippings enters in the oil refining cauldron 14, surveys the crude oil acid value, prepares alkali lye according to the crude oil acid value, and alkali number can be pressed column count:
G=(7.13×0.0001×F+B)×W÷C
G wherein: add alkali number, F: the acid value of the crude oil that remove, B: excess alkali quantity accounts for the heavy percentage ratio of oil, excess alkali quantity is generally the 0.3-0.5% of crude oil weight, W: oil is heavy, C: the percentage concentration of alkali lye, and the conversion relation of common alkali liquid degree Beaume and percentage concentration is as follows:
14 ° of Be are that 94.2%, 16 ° of Be is that 11.06%, 18 ° of Be is 12.59%.
In the alkali refining washing step, the processing parameter of alkali refining is: 5 tons of oil refining cauldron 14 oil capacitys, 65-70 ℃ of alkali refining oil temperature, 70 ℃ of alkali liquid temperatures, sedimentation time 6-8 hour, indirect steam pressure 0.4MPa; The processing parameter of washing is: amount of water is heavy by 10% for oil, 70 ℃ of softening water temperature, sedimentation time 4 hours, indirect steam pressure 0.4MPa.
Alkali lye is added in the oil refining cauldron 14, stirred 10 minutes, make alkali and oily thorough mixing, oily temperature rise to 65-70 ℃, was staticly settled 6-8 hour, with pump with the soap stock pump to soap stock jar 15, after sedimentation, soap stock put into soap stock pond 20.Oil is heated to 65-70 ℃, the softening water (or concentration is 5% salt solution) that adds 70 ℃ in oil washs, the softening water add-on is that oil is heavy by 10%, after staticly settling 4 hours, (as using salt solution, then staticly settling required time can shorten) bleeds off bottom waste water, soap stock is pumped into soap stock jar 15, after sedimentation, soap stock put into soap stock pond 20.Can repeat washing more once according to saponified matter content in the oil.Then, open water jet pump 17, make oil suck water trap 16, the processing parameter of water trap 16 is: 5 tons of water trap treatment capacities, (0.09MPa), dehydration temperaturre 90-100 ℃ of water trap vacuum tightness 710mmHg, dewatering time 2 hours, indirect steam pressure 0.4MPa, open steam pressure 0.05MPa.Through the crude oil of water trap 16 dehydrations, through entering finished product crude oil jar 19 after filter 18 filtrations.
Claims (5)
1, a kind of method of extracting raw corn oil from vinasse is characterized in that it comprises that successively the following technology step is poly-: heat, leaching, evaporation, stripping, alkali refining washing, sedimentation, dehydration, filtration are given in vinasse centrifugation, evaporation drying, granulation, oven dry.
2, the method for extracting raw corn oil from vinasse according to claim 1, it is characterized in that: the particle of granulation is 8-10mm.
3, the method for extracting raw corn oil from vinasse according to claim 1, it is characterized in that: extraction temperature is 50-55 ℃.
4, the method for extracting raw corn oil from vinasse according to claim 1, it is characterized in that: stripping mixing oil temperature out is 110-115 ℃.
5, the method for extracting raw corn oil from vinasse according to claim 1 is characterized in that: the solvent oil that evaporate, stripping comes out and the solvent oil reuse of mixing steam after condensation divides water of water.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN00101787A CN1307093A (en) | 2000-02-02 | 2000-02-02 | Method for extracting raw corn oil from distillers' grains |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN00101787A CN1307093A (en) | 2000-02-02 | 2000-02-02 | Method for extracting raw corn oil from distillers' grains |
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| CN1307093A true CN1307093A (en) | 2001-08-08 |
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| CN00101787A Pending CN1307093A (en) | 2000-02-02 | 2000-02-02 | Method for extracting raw corn oil from distillers' grains |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104593140A (en) * | 2015-01-22 | 2015-05-06 | 贵州华清科维环境能源有限责任公司 | Process for extracting vegetable oil from distiller grains |
| CN106367200A (en) * | 2016-11-15 | 2017-02-01 | 朝阳丰源生物科技有限公司 | Method for increasing oil extraction rate of sea buckthorn fruit peel residues |
| CN109793260A (en) * | 2019-01-30 | 2019-05-24 | 四川中烟工业有限责任公司 | A kind of spirit distiller grain oil and its preparation method and application |
| RU2809805C1 (en) * | 2021-07-12 | 2023-12-19 | Федеральное государственное бюджетное научное учреждение "Всероссийский научно-исследовательский институт жиров" | Column apparatus for distillation of oil miscellas |
-
2000
- 2000-02-02 CN CN00101787A patent/CN1307093A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104593140A (en) * | 2015-01-22 | 2015-05-06 | 贵州华清科维环境能源有限责任公司 | Process for extracting vegetable oil from distiller grains |
| CN106367200A (en) * | 2016-11-15 | 2017-02-01 | 朝阳丰源生物科技有限公司 | Method for increasing oil extraction rate of sea buckthorn fruit peel residues |
| CN109793260A (en) * | 2019-01-30 | 2019-05-24 | 四川中烟工业有限责任公司 | A kind of spirit distiller grain oil and its preparation method and application |
| RU2809805C1 (en) * | 2021-07-12 | 2023-12-19 | Федеральное государственное бюджетное научное учреждение "Всероссийский научно-исследовательский институт жиров" | Column apparatus for distillation of oil miscellas |
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