CN105950279A - Method and system for extracting grease from oil - Google Patents
Method and system for extracting grease from oil Download PDFInfo
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- CN105950279A CN105950279A CN201610407559.5A CN201610407559A CN105950279A CN 105950279 A CN105950279 A CN 105950279A CN 201610407559 A CN201610407559 A CN 201610407559A CN 105950279 A CN105950279 A CN 105950279A
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- 238000000034 method Methods 0.000 title claims abstract description 45
- 239000004519 grease Substances 0.000 title abstract description 9
- 239000002904 solvent Substances 0.000 claims abstract description 75
- 239000007788 liquid Substances 0.000 claims abstract description 65
- 239000000463 material Substances 0.000 claims abstract description 54
- 239000012046 mixed solvent Substances 0.000 claims abstract description 52
- 238000000605 extraction Methods 0.000 claims abstract description 42
- 239000001273 butane Substances 0.000 claims abstract description 17
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims abstract description 17
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000012530 fluid Substances 0.000 claims abstract description 9
- 239000012535 impurity Substances 0.000 claims abstract description 4
- 239000003921 oil Substances 0.000 claims description 99
- 235000014593 oils and fats Nutrition 0.000 claims description 50
- 238000011084 recovery Methods 0.000 claims description 31
- 241000196324 Embryophyta Species 0.000 claims description 24
- 239000000284 extract Substances 0.000 claims description 21
- 210000000582 semen Anatomy 0.000 claims description 18
- 230000000740 bleeding effect Effects 0.000 claims description 7
- 238000002360 preparation method Methods 0.000 claims description 7
- 210000001161 mammalian embryo Anatomy 0.000 claims description 6
- 230000008447 perception Effects 0.000 claims description 6
- 235000005637 Brassica campestris Nutrition 0.000 claims description 5
- 241001301148 Brassica rapa subsp. oleifera Species 0.000 claims description 5
- 239000003795 chemical substances by application Substances 0.000 claims description 5
- 238000005096 rolling process Methods 0.000 claims description 5
- 235000020238 sunflower seed Nutrition 0.000 claims description 5
- 238000001556 precipitation Methods 0.000 claims description 4
- MJYQFWSXKFLTAY-OVEQLNGDSA-N (2r,3r)-2,3-bis[(4-hydroxy-3-methoxyphenyl)methyl]butane-1,4-diol;(2r,3r,4s,5s,6r)-6-(hydroxymethyl)oxane-2,3,4,5-tetrol Chemical compound OC[C@H]1O[C@@H](O)[C@H](O)[C@@H](O)[C@@H]1O.C1=C(O)C(OC)=CC(C[C@@H](CO)[C@H](CO)CC=2C=C(OC)C(O)=CC=2)=C1 MJYQFWSXKFLTAY-OVEQLNGDSA-N 0.000 claims description 3
- 241000218236 Cannabis Species 0.000 claims description 3
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 235000004426 flaxseed Nutrition 0.000 claims description 3
- 238000010298 pulverizing process Methods 0.000 claims description 3
- 238000009825 accumulation Methods 0.000 claims 1
- 238000005086 pumping Methods 0.000 claims 1
- 230000008569 process Effects 0.000 abstract description 11
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 239000000203 mixture Substances 0.000 abstract description 3
- 238000004064 recycling Methods 0.000 abstract 1
- 239000013557 residual solvent Substances 0.000 abstract 1
- 230000009466 transformation Effects 0.000 description 7
- 238000000638 solvent extraction Methods 0.000 description 6
- 230000007704 transition Effects 0.000 description 4
- 150000001335 aliphatic alkanes Chemical class 0.000 description 3
- 231100000252 nontoxic Toxicity 0.000 description 3
- 230000003000 nontoxic effect Effects 0.000 description 3
- 239000000346 nonvolatile oil Substances 0.000 description 3
- 238000011160 research Methods 0.000 description 3
- 238000000194 supercritical-fluid extraction Methods 0.000 description 3
- LVGUZGTVOIAKKC-UHFFFAOYSA-N 1,1,1,2-tetrafluoroethane Chemical compound FCC(F)(F)F LVGUZGTVOIAKKC-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003925 fat Substances 0.000 description 2
- 239000003063 flame retardant Substances 0.000 description 2
- 150000002632 lipids Chemical class 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000003801 milling Methods 0.000 description 2
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 240000000528 Ricinus communis Species 0.000 description 1
- 235000004443 Ricinus communis Nutrition 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 239000002932 luster Substances 0.000 description 1
- 239000002480 mineral oil Substances 0.000 description 1
- 235000010446 mineral oil Nutrition 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 150000003904 phospholipids Chemical class 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 230000009967 tasteless effect Effects 0.000 description 1
- 230000008542 thermal sensitivity Effects 0.000 description 1
Classifications
-
- 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
- C11B1/06—Production of fats or fatty oils from raw materials by pressing
-
- 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
- C11B3/00—Refining fats or fatty oils
Abstract
The invention relates to a method and system for extracting grease from oil. The method for extracting grease from oil includes the following steps that firstly, the system for extracting grease from oil is prepared; secondly, materials are extracted, wherein after the materials to be extracted are subjected to impurity removal, germ flattening or smashing, the materials are conveyed into an extraction tank through a feeding pipe, a mixed solvent composed of liquid R134a and butane is discharged from the solvent tank, and the mixture solvent penetrates through a lower sieve plate and then makes contact with the materials to be extracted; thirdly, oil and the solvent are separated; fourthly, oil and material residual solvents are removed, and the extracted oil is discharged. By means of the method and system, extraction safety of subcritical fluid can be remarkably improved, phase change does not exist in the solvent recycling process, and energy consumption is greatly reduced.
Description
Technical field
The present invention relates to a kind of extract the method and system of oils and fats in oil plant, be specifically related to one and utilize low boiling alkane and derivative
The method of thing oil and grease extracting, and realize the system of the method.
Background technology
The preparation method of oils and fats mainly has milling process and solvent extraction method.Milling process takes oil and is made by mechanical external force effect, by oils and fats from oil
The method for extracting oil squeezed out in material, for the most expressed oils, generally need to roll oil plant embryo, 120 DEG C of high temperature steaming stir-frys, not only disappear
Consume a large amount of electric power and steam, and cause that crude oil color and luster is deep, acid number and non-hydratable phospholipid content high, Oxidation of Fat and Oils is serious.Leach
Method carries the solvent of oil use predominantly " No. six solvents ", and it is mainly composed of n-hexane, and its precipitation temperature is up to more than 110 DEG C,
Cause cake protein quality deterioration and thermal sensitivity nutrient loss.Supercritical CO2Extraction is an emerging oils and fats extractive technique, adopts
Use CO2As nontoxic solvent, tasteless, non-combustible, product organic solvent-free remains；Extraction conditions is the gentleest, can be to greatest extent
Ground retains the advantages such as natural constituent.But, in order to reach higher oil extraction efficiency, supercritical CO2Extracting pressure is general
Needing higher than 30MPa, to equipment requirements height, investment greatly, operation energy consumption is high.
Due to present stage supercritical extraction technique exist variety of problems, it is difficult to be applied to large-scale production, therefore seek green,
Low consumption and efficient oil extraction novel technique, become oils and fats in recent years and extract the study hotspot in field.Subcritical fluid extraction
Technology, as a kind of potential, scheme of alternative supercritical extraction technique, at home and abroad achieves under the effort of researcher
Many progress.Subcritical fluid extraction in addition to the advantage with supercritical extraction (nontoxic, harmless, environmental protection, pollution-free,
Non-thermal technology, the active component retaining extract does not destroys, does not aoxidizes), also solve that supercritical extracting equipment volume is little, make
Valency is high, be not suitable for the defect of large-scale industrial production.But, the subcritical solvent that conventional oil extraction efficiency is high is mainly fourth
Alkane, propane etc., these subcritical solvents are inflammable and explosive, and solvent recovery process exists phase transformation, cause energy consumption of a relatively high.
R134a (1,1,1,2-tetrafluoroethane) exists as a kind of inert, non-flammable and non-toxic, colorless environmental protection refrigerant
Countries in the world large-scale application, also gradually spreads out as the research of extractant it.But, research finds subcritical R134a
Poor to the dissolubility of oils and fats, it is applied to extracting pressure during lipid extraction higher (6MPa～12MPa), greatly limit it at oil
Fat processing is applied.R134a is in fact a more weak solvent for most of components, particularly non-volatile to some
Property component.R134a can be easy to from plant base material extract quintessence oil, without dissolving in more plant base material often with depositing
Fixed oil.Amazing, it has been found that R134a, although to fixed oil and mineral oil be at low temperatures one bad
Solvent, but can will improve the solvent nature of R134a largely under conditions of heating up.For the characteristic of institute's extract solutes,
Main extractant adds this preferable entrainer of solute extraction effect is carried out synergic solvent extraction, subcritical abstraction can be substantially improved
Performance.There are some researches show that R134a can effectively reduce the combustion range of flammable working medium as fire retardant or completely inhibit its combustion
Burn.Therefore, in R134a, add that a certain proportion of butane is collaborative carries out subcritical abstraction, be not only expected to improve low pressure conditions
The lower R134a extraction ability to lipid, and will be greatly improved than being used alone butane extraction safety.
Summary of the invention
The deficiency existed for existing oil extraction technology, it is an object of the invention to provide and a kind of extract the method for oils and fats in oil plant
With the safety that system, the method and system are remarkably improved subcritical fluid extraction, there is not phase transformation, greatly in solvent recovery process
Amplitude reduction energy expenditure.
For achieving the above object, the technical solution used in the present invention is, a kind of extracts the method for oils and fats in oil plant, including as follows
Step:
1) a kind of the preparation of the system of oils and fats in oil plant is extracted: a kind of extract the system of oils and fats in oil plant, including solvent tank, solvent
Pump, preheater, extractor, precooler, settling tank, oil tank, residual molten recovery unit gentle power conveying unit；Described is molten
The top and bottom of agent tank is correspondingly provided with inlet, liquid outlet；The top and bottom of described oil tank be correspondingly provided with inlet,
Liquid outlet；
Bottom described solvent tank, liquid outlet is connected with the inlet of solvent pump through pipeline and the 4th valve V4, the liquid outlet of solvent pump
Being connected with the inlet of preheater through pipeline and the 3rd valve V3, the liquid outlet of preheater is through pipeline and the second valve V2 and extraction
The inlet 1-10 of tank is connected, and the liquid outlet 1-9 of extractor is connected with the inlet of precooler through pipeline, the liquid outlet of precooler
Being connected with the inlet 2-7 of settling tank through pipeline and the 5th valve V5, the oil-out 2-6 of settling tank is through pipeline and the 6th valve
V6 is connected with oil tank top inlet, and the liquid outlet 2-11 of settling tank is through pipeline and the 7th valve V7 and solvent tank top feed liquor
Mouth is connected, and bottom oil tank, liquid outlet is provided with the 8th valve V8；
Extractor is provided with feed pipe 1-4, feed pipe 1-4 and is provided with the first valve V1；The liquid outlet 1-9 of extractor is through pipeline
It is connected with residual molten recovery unit with the tenth valve V10；The bleeding point 2-9 of settling tank is molten with residual through pipeline and the 11st valve V11
Recovery unit is connected；Oil tank top inlet is connected with residual molten recovery unit through pipeline and the 12nd valve V12；
Described air conveying unit is connected with the discharge nozzle 1-5 of extractor through pipeline and the 9th valve V9；
2) materials abstraction: material to be extracted, through remove impurity, after rolling embryo or pulverizing, opens the first valve V1, will through feed pipe 1-4
Material is conveyed in extractor, closes the first valve V1, open the second valve V2, the 3rd valve V3, the 5th valve V5, the tenth
Valve V10, the 11st valve V11, the 12nd valve V12, start the vacuum pump in residual molten recovery unit, by extractor, sinks
After fall tank and oil tank evacuation, then close the tenth valve V10, the 11st valve V11, the 12nd valve V12 and vacuum successively
Pump；Opening the 4th valve V4, the mixed solvent being made up of liquid R134a and butane is released from solvent tank, pumps into through solvent pump
Raising uniform temperature (25～45 DEG C) in preheater and enter in extractor by inlet 1-10, mixed solvent passes lower sieve plate
Contacting with material to be extracted after 1-8, by chuck 1-6, (interior circulation cycle is hot in extractor for mixed solvent and material to be extracted
Water) it is further heated to uniform temperature (35～55 DEG C), mixed solvent, the mixed solvent of heat is constantly pumped along with solvent pump
Gradually submergence material arrive liquid outlet 1-9 through upper sieve plate 1-7 in extraction process, and flows into precooler, and material due to
Limited by upper sieve plate and lower sieve plate, continue to be deposited in extractor；
3) oil separates with solvent: after in precooler, the mixed solvent of heat is lowered the temperature, in inlet 2-7 flows into settling tank,
After through the coil pipe 2-8 (interior circulation cycle coolant body) of settling tank, cooling is reduced to uniform temperature (-10 DEG C～20 DEG C) further,
The oil (oils and fats) dissolved in mixed solvent starts precipitation and floats over upper strata, and oil gathers on upper strata and overflows to oil spilling groove the most afterwards
In 2-5, when the oils and fats liquid level in liquidometer 2-10 perception oil spilling groove 2-5 is higher than preset height, united opening the 6th valve V6,
Make oils and fats temporary in oil-out 2-6 flows into oil tank, when liquidometer 2-10 perception oils and fats liquid level is less than preset height, linkage
Close the 6th valve V6, make oils and fats accumulate in oil spilling groove 2-5, the most repeatedly；The most separated out molten oils and fats purer
Mixed solvent sink, observable situation from visor 2-4, when purer mixed solvent runs up to a certain degree (visor absolute altitude
Half) after, open the 7th valve V7, purer mixed solvent is put into solvent tank from liquid outlet 2-11 and recycles；
4) oil and the residual solution-off of material are removed: after extraction completes, and close the 5th valve V5, the 7th valve V7, and reversion solvent pump is (molten
Agent pump inverts) remaining liquid solvent, to after in solvent tank, closes solvent pump, the 3rd valve V3, the 4th valve in extraction extractor
V4, opens the tenth valve V10, the 11st valve V11, the 12nd valve V12 and residual molten recovery unit, successively by extractor
Material and oil tank in residual contained by oil mixed solvent suction, compress and condensation is reclaimed and recycled into solvent tank；Residual
After solution-off has been removed, close the tenth valve V10, the 11st valve V11, the 12nd valve V12 and residual molten recovery unit successively；
Open the 9th valve V9, the material after extraction is pumped out extractor through air conveying unit；Open the 8th valve V8, will extraction
Oils and fats release.
Described extractor includes cylinder 1-1, top cover 1-2 and bottom 1-3, and top cover 1-2 is provided with liquid outlet 1-9, top cover 1-2
Being connected with cylinder 1-1 upper end through flange, in cylinder 1-1, upper end is provided with upper sieve plate 1-7, near upper sieve plate 1-7 lower left
Cylinder 1-1 outer wall is provided with feed pipe 1-4 (feed pipe is connected) with the cavity in cylinder, and feed pipe 1-4 is provided with the first valve
Door V1, in cylinder 1-1, lower end is provided with lower sieve plate 1-8, and the cylinder 1-1 outer wall near lower sieve plate 1-8 upper left is provided with discharging
Pipe 1-5 (discharge nozzle is connected with the cavity in cylinder), covers outside the cylinder 1-1 between feed pipe 1-4 and discharge nozzle 1-5
It is stamped chuck 1-6, bottom 1-3 to be provided with inlet 1-10, top cover 1-3 and be connected with cylinder 1-1 lower end through flange.
Described settling tank includes cylinder 2-1, top cover 2-2 and bottom 2-3, and top cover 2-2 is provided with bleeding point 2-9, top cover 2-2
Being connected with cylinder 2-1 upper end through flange, cylinder 2-1 outer upper end is provided with strip visor 2-4, near regarding inside cylinder 2-1
Mirror 2-4 is provided with oil spilling groove 2-5, and the cylinder 2-1 outer wall above the bottom surface of oil spilling groove 2-5 is provided with oil-out 2-6, in cylinder 2-1
Portion's outer wall is provided with inlet 2-7, is provided with coil pipe 2-8, coil pipe 2-8 and extends to lower end in the middle part of cylinder 2-1 in cylinder 2-1,
Bottom 2-3 is provided with liquid outlet 2-11, top cover 2-3 and is connected with cylinder 2-1 lower end through flange, and top cover 2-2 is additionally provided with liquidometer
2-10。
Residual molten recovery unit, air conveying unit are existing conventional techniques.Residual molten recovery unit is by vacuum pump, compression
Machine and condenser composition.Air conveying unit is made up of blower fan, cyclone separator and airlock.
By such scheme, material to be extracted be specially Brassica campestris L press cake, Semen Brassicae campestris, sunflower seed, Semen Ricini, Semen arachidis hypogaeae, Semen Camelliae,
Flaxseed, Fructus Cannabis or Semen sojae atricolor and press cake thereof.
By such scheme, the mass ratio that in mixed solvent, R134a mixes with butane is 1.5:1～9:1.
By such scheme, temperature when mixed solvent extracts in extractor is 35～55 DEG C, temperature when settling in settling tank
For-10 DEG C～20 DEG C.
By such scheme, mixed solvent pressure in extractor, settling tank is 0.1MPa～2MPa.
The invention has the beneficial effects as follows:
1) present invention uses R134a (HFA 134a) and butane to mix as solvent, and it dissolves oils and fats ability
Variation with temperature is very big, and available temperature difference carries out solvent recovery, and removal process, without phase transformation, can be greatly lowered energy expenditure,
Save production cost.
2) R134a has flame-retarding characteristic, in the case of the solvent inflammable with some mixes and mass ratio is dominant, as mixed with butane
Close, for greatly strengthen the safety of production and reduce the danger of blast.
3) R134a and butane are gaseous state at normal temperatures and pressures, easily liquefy after pressurization, and extraction temperature and de-residual solubility temperature are the lowest,
The active component in material and oils and fats can be maintained to greatest extent.
Accompanying drawing explanation
Fig. 1 is the process chart of the present invention.
Fig. 2 is the structural representation of extractor of the present invention.
Fig. 3 is the structural representation of settling tank of the present invention.
In Fig. 2: cylinder 1-1, top cover 1-2, bottom 1-3, feed pipe 1-4, discharge nozzle 1-5, chuck 1-6, upper sieve plate
1-7, lower sieve plate 1-8, liquid outlet 1-9, inlet 1-10
In Fig. 3: cylinder 2-1, top cover 2-2, bottom 2-3, visor 2-4, oil spilling groove 2-5, oil-out 2-6, inlet
2-7, coil pipe 2-8, bleeding point 2-9, liquidometer 2-10, liquid outlet 2-11
Detailed description of the invention
The preferred version of the present invention is described below in conjunction with the accompanying drawings；Within it is included in the scope of protection of the invention, but it is not intended to this
Invention.
Embodiment 1 (oil and grease extracting in Brassica campestris L press cake):
As Figure 1-3, a kind of extract the method for oils and fats in oil plant, comprise the steps:
1) a kind of the preparation of the system of oils and fats in oil plant is extracted: a kind of extract the system of oils and fats in oil plant, including solvent tank, solvent
Pump, preheater, extractor, precooler, settling tank, oil tank, residual molten recovery unit (or claim solvent recovery unit) are gentle
Power conveying unit (or claiming pneumatic transport equipment)；The top and bottom of described solvent tank is correspondingly provided with inlet, liquid outlet；
The top and bottom of described oil tank is correspondingly provided with inlet, liquid outlet；
Bottom described solvent tank, liquid outlet is connected with the inlet of solvent pump through pipeline and the 4th valve V4, the liquid outlet of solvent pump
Being connected with the inlet of preheater through pipeline and the 3rd valve V3, the liquid outlet of preheater is through pipeline and the second valve V2 and extraction
The inlet 1-10 of tank is connected, and the liquid outlet 1-9 of extractor is connected with the inlet of precooler through pipeline, the liquid outlet of precooler
Being connected with the inlet 2-7 of settling tank through pipeline and the 5th valve V5, the oil-out 2-6 of settling tank is through pipeline and the 6th valve
V6 is connected with oil tank top inlet, and the liquid outlet 2-11 of settling tank is through pipeline and the 7th valve V7 and solvent tank top feed liquor
Mouth is connected, and bottom oil tank, liquid outlet is provided with the 8th valve V8；
The liquid outlet 1-9 of extractor, the bleeding point 2-9 of settling tank, oil tank top inlet are respectively through pipeline and valve the (the tenth
Valve V10, the 11st valve V11, the 12nd valve V12) it is connected with residual molten recovery unit；
Described air conveying unit is connected with the discharge nozzle 1-5 of extractor through pipeline and the 9th valve V9；
Described extractor includes cylinder 1-1, top cover 1-2 and bottom 1-3, and top cover 1-2 is provided with liquid outlet 1-9, top cover 1-2
Being connected with cylinder 1-1 upper end through flange, in cylinder 1-1, upper end is provided with upper sieve plate 1-7, near upper sieve plate 1-7 lower left
Cylinder 1-1 outer wall is provided with feed pipe 1-4 (feed pipe is connected) with the cavity in cylinder, and feed pipe 1-4 is provided with the first valve
Door V1, in cylinder 1-1, lower end is provided with lower sieve plate 1-8, and the cylinder 1-1 outer wall near lower sieve plate 1-8 upper left is provided with discharging
Pipe 1-5 (discharge nozzle is connected with the cavity in cylinder), covers outside the cylinder 1-1 between feed pipe 1-4 and discharge nozzle 1-5
It is stamped chuck 1-6, bottom 1-3 to be provided with inlet 1-10, top cover 1-3 and be connected with cylinder 1-1 lower end through flange；
Described settling tank includes cylinder 2-1, top cover 2-2 and bottom 2-3, and top cover 2-2 is provided with bleeding point 2-9, top cover 2-2
Being connected with cylinder 2-1 upper end through flange, cylinder 2-1 outer upper end is provided with strip visor 2-4, near regarding inside cylinder 2-1
Mirror 2-4 is provided with oil spilling groove 2-5, and the cylinder 2-1 outer wall above the bottom surface of oil spilling groove 2-5 is provided with oil-out 2-6, in cylinder 2-1
Portion's outer wall is provided with inlet 2-7, is provided with coil pipe 2-8, coil pipe 2-8 and extends to lower end in the middle part of cylinder 2-1 in cylinder 2-1,
Bottom 2-3 is provided with liquid outlet 2-11, top cover 2-3 and is connected with cylinder 2-1 lower end through flange, and top cover 2-2 is additionally provided with liquidometer
2-10；
Residual molten recovery unit, air conveying unit are existing conventional techniques；Residual molten recovery unit is by vacuum pump, compression
Machine and condenser composition；Air conveying unit is made up of blower fan, cyclone separator and airlock；
2) materials abstraction: material to be extracted, through remove impurity, after rolling embryo or pulverizing, opens the first valve V1, will through feed pipe 1-4
Material is conveyed in extractor, closes the first valve V1, open the second valve V2, the 3rd valve V3, the 5th valve V5, the tenth
Valve V10, the 11st valve V11, the 12nd valve V12, start the vacuum pump in residual molten recovery unit, by extractor, sinks
After fall tank and oil tank evacuation, then close the tenth valve V10, the 11st valve V11, the 12nd valve V12 and vacuum successively
Pump；Opening the 4th valve V4, the mixed solvent being made up of liquid R134a and butane is released from solvent tank, pumps into through solvent pump
Raising uniform temperature (25～45 DEG C) in preheater and enter in extractor by inlet 1-10, mixed solvent passes lower sieve plate
Contacting with material to be extracted after 1-8, by chuck 1-6, (interior circulation cycle is hot in extractor for mixed solvent and material to be extracted
Water) it is further heated to uniform temperature (35～55 DEG C), mixed solvent, the mixed solvent of heat is constantly pumped along with solvent pump
Gradually submergence material arrive liquid outlet 1-9 through upper sieve plate 1-7 in extraction process, and flows into precooler, and material due to
Limited by upper sieve plate and lower sieve plate, continue to be deposited in extractor；
3) oil separates with solvent: after in precooler, the mixed solvent of heat is lowered the temperature, in inlet 2-7 flows into settling tank,
After through the coil pipe 2-8 (interior circulation cycle coolant body) of settling tank, cooling is reduced to uniform temperature (-10 DEG C～20 DEG C) further,
The oil (oils and fats) dissolved in mixed solvent starts precipitation and floats over upper strata, and oil gathers on upper strata and overflows to oil spilling groove the most afterwards
In 2-5, when the oils and fats liquid level in liquidometer 2-10 perception oil spilling groove 2-5 is higher than preset height, united opening the 6th valve V6,
Make oils and fats temporary in oil-out 2-6 flows into oil tank, when liquidometer 2-10 perception oils and fats liquid level is less than preset height, linkage
Close the 6th valve V6, make oils and fats accumulate in oil spilling groove 2-5, the most repeatedly；The most separated out molten oils and fats purer
Mixed solvent sink, observable situation from visor 2-4, when purer mixed solvent runs up to a certain degree (visor absolute altitude
Half) after, open the 7th valve V7, purer mixed solvent is put into solvent tank from liquid outlet 2-11 and recycles；
4) oil and the residual solution-off of material are removed: after extraction completes, and close the 5th valve V5, the 7th valve V7, and reversion solvent pump is (molten
Agent pump inverts) remaining liquid solvent, to after in solvent tank, closes solvent pump, the 3rd valve V3, the 4th valve in extraction extractor
V4, opens the tenth valve V10, the 11st valve V11, the 12nd valve V12 and residual molten recovery unit, successively by extractor
Material and oil tank in the mixed solvent of residual contained by oil aspirated by residual molten recovery unit, compress and condensation is reclaimed into molten
Agent tank recycles；After residual solution-off has been removed, close the tenth valve V10, the 11st valve V11, the 12nd valve V12 successively
With residual molten recovery unit；Open the 9th valve V9, the material after extraction is pumped out extractor through air conveying unit；Open the
Eight valve V8, release the oils and fats (or claiming oil) of extraction.
By such scheme, material to be extracted be specially Brassica campestris L press cake, Semen Brassicae campestris, sunflower seed, Semen Ricini, Semen arachidis hypogaeae, Semen Camelliae,
Flaxseed, Fructus Cannabis or Semen sojae atricolor and press cake thereof.
By such scheme, the mass ratio that in mixed solvent, R134a mixes with butane is 1.5:1～9:1.
By such scheme, temperature when mixed solvent extracts in extractor is 35～55 DEG C, temperature when settling in settling tank
For-10 DEG C～20 DEG C.
By such scheme, mixed solvent pressure in extractor, settling tank is 0.1MPa～2MPa.
By such scheme, step 2) in materials abstraction: material be pulverize Brassica campestris L press cake, R134a and fourth in mixed solvent
The mass ratio of alkane mixing is 1.5:1, and solvent extraction temperature in extractor is 50 DEG C, and extracting pressure is 1.8MPa, and remaining is same
On；
By such scheme, step 3) in oil separate with solvent: temperature when solvent settles in settling tank is 10 DEG C, and pressure is
0.2Mpa。
Owing to flammable butane only accounts for the 10%～40% of butane and R134a mixed solvent, R134a can have enough as fire retardant
Amount stop mixed solvent occur burning and blast.Therefore the method and system are remarkably improved the safety of subcritical fluid extraction.
Most of mixed solvent of the method reclaims all in the recovery that is in a liquid state, and its extraction process is also carried out in liquid condition, because of
There is not phase transition process in this, energy expenditure can be greatly lowered to about the 1/2 of conventional phase transformation removal process.
Embodiment 2 (oil and grease extracting in Semen Brassicae campestris):
1) a kind of the preparation of the system of oils and fats in oil plant is extracted: with embodiment 1；
2) materials abstraction: material is the Semen Brassicae campestris rolling embryo, the mass ratio that in mixed solvent, R134a mixes with butane is 1.7:1,
Solvent extraction temperature in extractor is 45 DEG C, and extracting pressure is 1.6MPa, and remaining is with embodiment 1；
3) oil separates with solvent: temperature when solvent settles in settling tank is 5 DEG C, and pressure is 0.15MPa；
4) oil and the residual solution-off of material are removed: with embodiment 1.
Therefore the method and system are remarkably improved the safety of subcritical fluid extraction.Most of mixed solvent of the method reclaims
All in the recovery that is in a liquid state, its extraction process is also carried out in liquid condition, the most there is not phase transition process, can be significantly
Reduce energy expenditure to about the 1/2 of conventional phase transformation removal process.
Embodiment 3 (oil and grease extracting in sunflower seed):
1) a kind of the preparation of the system of oils and fats in oil plant is extracted: ibid；
2) materials abstraction: material is the sunflower seed rolling embryo, the mass ratio that in mixed solvent, R134a mixes with butane is 2:1,
Solvent extraction temperature in extractor is 55 DEG C, and extracting pressure is 2MPa, and remaining is ibid；
3) oil separates with solvent: temperature when solvent settles in settling tank is-10 DEG C, and pressure is 0.05MPa；
4) oil and the residual solution-off of material are removed: ibid.
Therefore the method and system are remarkably improved the safety of subcritical fluid extraction.Most of mixed solvent of the method reclaims
All in the recovery that is in a liquid state, its extraction process is also carried out in liquid condition, the most there is not phase transition process, can be significantly
Reduce energy expenditure to about the 1/2 of conventional phase transformation removal process.
Embodiment 4 (oil and grease extracting in Semen Ricini):
1) a kind of the preparation of the system of oils and fats in oil plant is extracted: ibid；
2) materials abstraction: material is the castor bean pulverized, and the mass ratio that in mixed solvent, R134a mixes with butane is 9:1,
Solvent extraction temperature in extractor is 35 DEG C, and extracting pressure is 1.0MPa, and remaining is ibid；
3) oil separates with solvent: temperature when solvent settles in settling tank is 20 DEG C, and pressure is 0.5MPa；
4) oil and the residual solution-off of material are removed: ibid.
Therefore the method and system are remarkably improved the safety of subcritical fluid extraction.Most of mixed solvent of the method reclaims
All in the recovery that is in a liquid state, its extraction process is also carried out in liquid condition, the most there is not phase transition process, can be significantly
Reduce energy expenditure to about the 1/2 of conventional phase transformation removal process.
Claims (7)
1. one kind extracts the method for oils and fats in oil plant, it is characterised in that comprise the steps:
1) a kind of the preparation of the system of oils and fats in oil plant is extracted: a kind of extract the system of oils and fats in oil plant, including solvent tank, solvent
Pump, preheater, extractor, precooler, settling tank, oil tank, residual molten recovery unit gentle power conveying unit；Described is molten
The top and bottom of agent tank is correspondingly provided with inlet, liquid outlet；The top and bottom of described oil tank be correspondingly provided with inlet,
Liquid outlet；
Bottom described solvent tank, liquid outlet is connected with the inlet of solvent pump through pipeline and the 4th valve (V4), going out of solvent pump
Liquid mouth is connected with the inlet of preheater through pipeline and the 3rd valve (V3), and the liquid outlet of preheater is through pipeline and the second valve (V2)
Being connected with the inlet (1-10) of extractor, the liquid outlet (1-9) of extractor is connected with the inlet of precooler through pipeline, in advance
The liquid outlet of cooler is connected with the inlet (2-7) of settling tank through pipeline and the 5th valve (V5), the oil-out (2-6) of settling tank
Being connected with oil tank top inlet through pipeline and the 6th valve (V6), the liquid outlet (2-11) of settling tank is through pipeline and the 7th
Valve (V7) is connected with solvent tank top inlet, and bottom oil tank, liquid outlet is provided with the 8th valve (V8)；
Extractor is provided with feed pipe (1-4), and feed pipe (1-4) is provided with the first valve (V1)；The liquid outlet (1-9) of extractor
It is connected with residual molten recovery unit through pipeline and the tenth valve (V10)；The bleeding point (2-9) of settling tank is through pipeline and the 11st valve
Door (V11) is connected with residual molten recovery unit；Oil tank top inlet is through pipeline and the 12nd valve (V12) and residual molten recovery
Unit is connected；
Described air conveying unit is connected with the discharge nozzle (1-5) of extractor through pipeline and the 9th valve (V9)；
2) materials abstraction: material to be extracted, through remove impurity, after rolling embryo or pulverizing, opens the first valve (V1), through feed pipe (1-4)
Material is conveyed in extractor, closes the first valve (V1), open the second valve (V2), the 3rd valve (V3), the 5th valve
Door (V5), the tenth valve (V10), the 11st valve (V11), the 12nd valve (V12), start in residual molten recovery unit
Vacuum pump, after extractor, settling tank and oil tank evacuation, more successively close the tenth valve (V10), the 11st valve (V11),
12nd valve (V12) and vacuum pump；Open the 4th valve (V4), the mixed solvent being made up of liquid R134a and butane from
Solvent tank is released, in solvent pump pumps into preheater, rises high-temperature enter extractor through inlet (1-10) after 25～45 DEG C
In, mixed solvent contacts with material to be extracted afterwards through lower sieve plate (1-8), and mixed solvent and material to be extracted are at extractor
Middle it is further heated to temperature to 35～55 DEG C by chuck (1-6), constantly pumps mixed solvent along with solvent pump, heat mixed
Bonding solvent gradually submergence material arrive liquid outlet (1-9) through upper sieve plate (1-7) in extraction process, and flows into precooler,
And material is owing to being limited by upper sieve plate and lower sieve plate, continue to be deposited in extractor；
3) oil separates with solvent: after in precooler, the mixed solvent of heat is lowered the temperature, and flows into settling tank through inlet (2-7)
In, after through the coil pipe (2-8) of settling tank, cooling is reduced to temperature-10 DEG C～20 DEG C further, the oils and fats dissolved in mixed solvent
Starting precipitation and float over upper strata, oils and fats overflows in oil spilling groove (2-5), when in liquidometer (2-10) perception oil spilling groove (2-5)
Oils and fats liquid level higher than preset height time, united opening the 6th valve (V6), make oils and fats through oil-out (2-6) flow into oil tank
In temporary, when liquidometer (2-10) perception oils and fats liquid level is less than preset height, linkage is closed the 6th valve (V6), is made oils and fats
Accumulation in oil spilling groove (2-5), the most repeatedly；
The most separated out the purer mixed solvent of molten oils and fats sink, observable situation from visor (2-4), when purer
Mixed solvent run up to a certain degree after, open the 7th valve (V7), purer mixed solvent is put from liquid outlet (2-11)
Enter in solvent tank and recycle；
4) oil and the residual solution-off of material are removed: after extraction completes, and close the 5th valve (V5), the 7th valve (V7), invert solvent
Pumping takes in extractor remaining liquid solvent to after in solvent tank, closes solvent pump, the 3rd valve (V3), the 4th valve (V4),
Open the tenth valve (V10), the 11st valve (V11), the 12nd valve (V12) and residual molten recovery unit successively, will extraction
The mixed solvent suction of residual contained by oil in material in tank and oil tank, compress and condensation is reclaimed and recycled into solvent tank；
After residual solution-off has been removed, close the tenth valve (V10), the 11st valve (V11), the 12nd valve (V12) and residual molten successively
Reclaim unit；Open the 9th valve (V9), the material after extraction is pumped out extractor through air conveying unit；Open the 8th valve
Door (V8), releases the oils and fats of extraction.
The most according to claim 1 a kind of extract the method for oils and fats in oil plant, it is characterised in that described extractor includes
Cylinder (1-1), top cover (1-2) and bottom (1-3), top cover (1-2) is provided with liquid outlet (1-9), top cover (1-2) warp
Flange is connected with cylinder (1-1) upper end, and cylinder (1-1) interior upper end is provided with upper sieve plate (1-7), under upper sieve plate (1-7)
Cylinder (1-1) outer wall on the left of side is provided with feed pipe (1-4), and feed pipe is connected with the cavity in cylinder, feed pipe (1-4)
Being provided with the first valve (V1), cylinder (1-1) interior lower end is provided with lower sieve plate (1-8), near lower sieve plate (1-8) upper left
Cylinder (1-1) outer wall be provided with discharge nozzle (1-5), discharge nozzle is connected with the cavity in cylinder, feed pipe (1-4) and going out
Cylinder (1-1) outer side covers between material pipe (1-5) has chuck (1-6), bottom (1-3) to be provided with inlet (1-10),
Top cover (1-3) is connected with cylinder (1-1) lower end through flange.
The most according to claim 1 a kind of extract the method for oils and fats in oil plant, it is characterised in that described settling tank includes
Cylinder (2-1), top cover (2-2) and bottom (2-3), top cover (2-2) is provided with bleeding point (2-9), top cover (2-2) warp
Flange is connected with cylinder (2-1) upper end, and cylinder (2-1) outer upper end is provided with strip visor (2-4), in cylinder (2-1)
Side is provided with oil spilling groove (2-5) near visor (2-4), and cylinder (2-1) outer wall above the bottom surface of oil spilling groove (2-5) is provided with out
Hydraulic fluid port (2-6), cylinder (2-1) middle part outer wall is provided with inlet (2-7), is provided with coil pipe (2-8), dish in cylinder (2-1)
Pipe (2-8) extends to lower end from cylinder (2-1) middle part, and bottom (2-3) is provided with liquid outlet (2-11), top cover (2-3)
It is connected with cylinder (2-1) lower end through flange, top cover (2-2) is additionally provided with liquidometer (2-10).
The most according to claim 1 a kind of extract the method for oils and fats in oil plant, it is characterised in that material to be extracted is concrete
For Brassica campestris L press cake, Semen Brassicae campestris, sunflower seed, Semen Ricini, Semen arachidis hypogaeae, Semen Camelliae, flaxseed, Fructus Cannabis or Semen sojae atricolor and press cake thereof.
The most according to claim 1 a kind of extract the method for oils and fats in oil plant, it is characterised in that R134a in mixed solvent
The mass ratio mixed with butane is 1.5:1～9:1.
The most according to claim 1 a kind of extract the method for oils and fats in oil plant, it is characterised in that mixed solvent is at extractor
Temperature during middle extraction is 35～55 DEG C, and temperature when settling in settling tank is-10 DEG C～20 DEG C.
The most according to claim 1 a kind of extract the method for oils and fats in oil plant, it is characterised in that mixed solvent extractor,
Pressure in settling tank is 0.1MPa～2MPa.
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101306852A (en) * | 2008-05-13 | 2008-11-19 | 苏州工业园区姑苏科技有限公司 | Oil-water separation apparatus |
| CN101474493A (en) * | 2008-12-05 | 2009-07-08 | 符文飙 | Mixed solvent low-pressure fluid critical extract method |
| CN103349849A (en) * | 2013-07-22 | 2013-10-16 | 曹庸 | Multifunctional continuous phase transition extraction device |
| CN104004586A (en) * | 2014-05-09 | 2014-08-27 | 中国农业科学院油料作物研究所 | Subcritical fluid extraction method and apparatus for lipid |
| CN203938661U (en) * | 2014-05-09 | 2014-11-12 | 中国农业科学院油料作物研究所 | A kind of device of subcritical fluid extraction lipid |
| CN204193648U (en) * | 2014-10-11 | 2015-03-11 | 中国农业科学院油料作物研究所 | The retracting device of solvent in a kind of miscella |
| CN105130065A (en) * | 2015-10-14 | 2015-12-09 | 攀钢集团成都钢钒有限公司 | Treating system for oily sewage |
-
2016
- 2016-06-12 CN CN201610407559.5A patent/CN105950279A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101306852A (en) * | 2008-05-13 | 2008-11-19 | 苏州工业园区姑苏科技有限公司 | Oil-water separation apparatus |
| CN101474493A (en) * | 2008-12-05 | 2009-07-08 | 符文飙 | Mixed solvent low-pressure fluid critical extract method |
| CN103349849A (en) * | 2013-07-22 | 2013-10-16 | 曹庸 | Multifunctional continuous phase transition extraction device |
| CN104004586A (en) * | 2014-05-09 | 2014-08-27 | 中国农业科学院油料作物研究所 | Subcritical fluid extraction method and apparatus for lipid |
| CN203938661U (en) * | 2014-05-09 | 2014-11-12 | 中国农业科学院油料作物研究所 | A kind of device of subcritical fluid extraction lipid |
| CN204193648U (en) * | 2014-10-11 | 2015-03-11 | 中国农业科学院油料作物研究所 | The retracting device of solvent in a kind of miscella |
| CN105130065A (en) * | 2015-10-14 | 2015-12-09 | 攀钢集团成都钢钒有限公司 | Treating system for oily sewage |
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Application publication date: 20160921 |