CN106929162A - A kind of utilization waste grease produces the deacidification technique of glycerine - Google Patents
A kind of utilization waste grease produces the deacidification technique of glycerine Download PDFInfo
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- CN106929162A CN106929162A CN201710201592.7A CN201710201592A CN106929162A CN 106929162 A CN106929162 A CN 106929162A CN 201710201592 A CN201710201592 A CN 201710201592A CN 106929162 A CN106929162 A CN 106929162A
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- glycerine
- oil
- ester exchange
- methyl alcohol
- exchange reaction
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- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
- C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
- C11C3/04—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fats or fatty oils
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/18—Stationary reactors having moving elements inside
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/18—Stationary reactors having moving elements inside
- B01J19/1862—Stationary reactors having moving elements inside placed in series
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
-
- 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
- C11B13/00—Recovery of fats, fatty oils or fatty acids from waste materials
-
- 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
- C11B3/001—Refining fats or fatty oils by a combination of two or more of the means hereafter
-
- 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
- C11B3/12—Refining fats or fatty oils by distillation
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
- C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
- C11C3/04—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fats or fatty oils
- C11C3/06—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fats or fatty oils with glycerol
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
- C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
- C11C3/04—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fats or fatty oils
- C11C3/10—Ester interchange
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
-
- 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
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Wood Science & Technology (AREA)
- General Chemical & Material Sciences (AREA)
- Microbiology (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Fats And Perfumes (AREA)
Abstract
The present invention relates to the deacidification technique that a kind of utilization waste grease produces glycerine, waste grease is sent to static mixer one after being heated by raw oil pump, crude glycerine containing soap is pumped toward static mixer one after being heated from crude glycerine addition, feedstock oil carries out pre-esterification reactor after being sufficiently mixed by static mixer one with crude glycerine into pre-esterification reactor tower, crude glycerine is under soap catalytic action, glyceride is generated with the free-fat acid reaction in feedstock oil, making the acid value of feedstock oil reduces.Into being distilled in thin film evaporator, gaseous substance is separated the glyceride that pre-esterification reactor is obtained into vapour liquid separator, obtains the glycerine of more than 96%wt after condensed from the glycerin vapor of vapour liquid separator top discharge.From after the neutral oil cooling of thin film evaporator bottom discharge, NaOH and methyl alcohol are added, ester exchange reaction is carried out after mixing and obtains containing alcohol methyl esters, containing alcohol methyl esters obtains biodiesel through dealcoholysis.The technique can reduce corrosion, more environmentally friendly, energy-conservation and reduction production cost.
Description
Technical field
The present invention relates to the deacidification technique that a kind of utilization waste grease produces glycerine, belong to grease processing technology field.
Background technology
Non-renewable energy resources are increasingly reduced with people and environmental pollution concern increasingly, waste resource comprehensive utilization,
The raw material of industry of the friendly recyclable fuel of exploitation novel environmental or high value turned into current scientific research hot subject it
One.The substitute fuel that waste grease is converted into diesel oil is had the advantages that it is renewable and biodegradable, to mitigate atmospheric greenhouse
The economic sustainable development of gas concentration, the living environment for improving the mankind, realization has great importance.China has greatly every year
The waste grease of amount, makes full use of this quasi-grease to have economic worth very high, waste oil can be solved again and flows to dining table, threatens
The safe diet of people.But because this kind of acid value of oil and fat is high, impurity is more, complicated component, should not be directly used in and produce biological bavin
Oil, it is necessary to deacidification removal of impurities first is carried out to it.
Existing deacidification technique one:After impurity, colloid, moisture in removing feedstock oil, prepared using soda acid two-step method and given birth to
Thing diesel oil, addition sulfuric acid catalysis（Or other solid acids）, be passed through excessive methanol carries out pre-esterification with the free fatty in raw material
React reduce the acid value of raw material and take away generation moisture promote reaction carried out to positive direction, after fully being reacted through pre-esterification,
Adding NaOH, methyl alcohol carries out ester exchange reaction, and standing separation goes out by-product glycerin after reaction completely, after isolating glycerine,
Dealcoholysis, washing and drying, rectifying respectively must refine methyl esters.
Existing deacidification technique two：Raw material after pretreatment, it is free in removing raw material using the method for physical deacidification
After aliphatic acid, add NaOH, methyl alcohol to carry out ester exchange reaction, dealcoholysis after reaction completely, and standing separation to go out accessory substance sweet
After oil, washing and drying, rectifying must refine methyl esters.The free fatty and methyl alcohol generated through depickling are in P-TOLUENE SULFO ACID 99（Or other are urged
Agent）Fatty acid methyl ester is generated under catalytic condition.
Either deacidification technique one or deacidification technique two in existing process, all employ acid, inevitably cause and contain
The discharge of sour waste water, has greater environmental impacts.
Biodiesel process is prepared using soda acid two-step method, it is high to equipment material requirement, it is serious to corrosive pipeline, produce acid
Water causes environmental pollution, difficult treatment, and using solid catalyst high cost, catalytic effect is bad.Using gas-phase methanol pre-esterification
Reaction, the easy evaporating, emitting, dripping or leaking of liquid or gas of methanol steam easily causes loss, and methanol steam is poisonous, inflammable, easy leakage, is unfavorable for operating personnel's
It is healthy and high to workshop electrical equipment explosive-proof grade requirement.Phase transformation consumed energy during methanol gasifying, contains after excessive methanol is condensed
Need rectifying more water, energy higher need to be consumed, increase rectifying load and need substantial amounts of steam.
Free fatty, high energy consumption are deviate from using physical method；When the free fatty of abjection carries out esterification reaction of organic acid, first
Alcohol consumption is high, reacts the poor quality of the fatty acid methyl ester of generation；Technique is relative complex, the high cost that equipment puts into for the first time.
The content of the invention
It is an object of the present invention to overcome problems of the prior art, there is provided one kind produces sweet using waste grease
The deacidification technique of oil, it is possible to reduce the corrosion to equipment, reduces the generation of sour water, makes more environmentally friendly technique, energy-conservation and reduce production
Cost.
To solve above technical problem, a kind of utilization waste grease of the invention produces the deacidification technique of glycerine, including such as
Lower step：Waste grease after imurity-removal and moisture enters the quenched tank of feedstock oil, and static state is sent to by raw oil pump after being heated
Blender one, crude glycerine containing soap enters crude glycerine temporary storage tank, former from crude glycerine addition pumping toward static mixer one after being heated
Material oil carries out pre-esterification reactor after being sufficiently mixed by static mixer one with crude glycerine into pre-esterification reactor tower, and crude glycerine exists
Under soap catalytic action, glyceride is generated with the free-fat acid reaction in feedstock oil, making the acid value of feedstock oil reduces.
Relative to prior art, the present invention achieves following beneficial effect：In pre-esterification reactor tower, anhydrous
In the case of, crude glycerine generates glyceride under soap catalytic action with the free-fat acid reaction in feedstock oil, and course of reaction is：.The present invention is using base-catalyzed transesterification reaction
The crude glycerine of generation replaces the free-fat acid reaction in methyl alcohol and feedstock oil, the feedstock oil of acid value 22 can be down into less than 2,
Meet the requirement that the esterification of next step alkali is exchanged, can be used for the raw material of different acid value scopes, methanol consumption can be saved, reduce steam
Consumption, reduces sour water discharge, reduces equipment corrosion；Prevent methyl alcohol evaporating, emitting, dripping or leaking of liquid or gas, improve workshop security.In crude glycerine
Weak base soap adds catalyst as the catalyst of esterification without other；Operation safety and reliability, economic benefit is higher.
As improvement of the invention, during the pre-esterification reactor, moisture and small molecular weight impurity of the boiling point less than glycerine
Discharged from the gaseous phase outlet of the pre-esterification reactor tower.Using the boiling point of the boiling point higher than water of glycerine, in pre-esterification reactor tower
Temperature and negative pressure cause that boiling point shifts to an earlier date the gaseous phase outlet from pre-esterification reactor top of tower less than the moisture and small molecular weight impurity of glycerine
Discharge, it is ensured that follow-up workshop section can obtain the pure glycerine of comparing.
As a further improvement on the present invention, the glyceride that pre-esterification reactor is obtained is into being steamed in thin film evaporator
Evaporate, the gaseous substance that thin film evaporator is evaporated is separated into vapour liquid separator, steamed from the glycerine of vapour liquid separator top discharge
Vapour obtains the glycerine that mass fraction is more than 96% after being condensed through glycerine condenser.The present invention is i.e. available before alkali esterification is exchanged
The glycerine of mass fraction more than 96%, can sell as product of the invention, increase economic efficiency.
As a further improvement on the present invention, the quenched tank relaying of feedstock oil is returned to from the oil slick of vapour liquid separator bottom discharge
It is continuous to participate in circulation.The present invention has prevented the discharge of oil slick, it is to avoid the pollution of environment and the cost of subsequent treatment, improves the present invention
The yield of finished product and semi-finished product.
As a further improvement on the present invention, from after the neutral oil cooling of thin film evaporator bottom discharge, hydrogen is added
Sodium oxide molybdena and methyl alcohol, carry out ester exchange reaction and obtain containing alcohol into ester exchange reaction device jointly after mixing through static mixer two
Methyl esters, containing alcohol methyl esters obtains biodiesel through dealcoholysis.Reduce the neutral oil after acid value and be cooled to and meet the temperature that alkali esterification is exchanged
Afterwards, add NaOH as catalyst, ester exchange reaction entered using methyl alcohol and neutral oil, biodiesel is obtained after dealcoholysis,
Can be sold as product, make the present invention that there is economic benefit very high, it is higher that biodiesel can obtain purity through distillation
Smart methyl esters and pitch, allow waste grease to obtain the trans-utilization of high benefit, and very environmentally friendly in production process, contamination-free
Discharge and corrosive deposit generation.
As a further improvement on the present invention, the neutral oil from thin film evaporator bottom discharge is first quenched with feedstock oil
The feedstock oil of tank discharge carries out indirect heat exchange by heat exchanger, then the oil temperature of neutral oil is adjusted into anti-to ester exchange by water cooler
Answer required temperature.The neutral oil that thin film evaporator is discharged is cooled down using feedstock oil, complies with ester exchange reaction dress
Required temperature is put, the UTILIZATION OF VESIDUAL HEAT IN of neutral oil is realized, the load of road oil temperature cooling after mitigation, while feedstock oil can be improved
Temperature, reach the purpose of energy efficiency.
As a further improvement on the present invention, the ester exchange byproduct of the ester exchange reaction bottom of device discharge includes containing
The crude glycerine of methyl alcohol and a small amount of methyl esters, into after oil partition tank stratification, the methyl esters overflowed from upper strata returns to ester exchange reaction dress
Put circulation, crude glycerine of the oil partition tank bottom containing methyl alcohol is admitted to the centre entrance of methanol rectifying tower, methanol steam is from methanol rectification
It is extracted at the top of tower, liquid is turned into through methanol condenser condensation, into the methyl alcohol one that methyl alcohol temporary storage tank, methyl alcohol temporary storage tank are reclaimed
Part enters the refluxing opening of methanol rectification top of tower, and another part is returned in the ester exchange reaction device and circulated, crude glycerine from
The bottom discharge of methanol rectifying tower.There is minimal amount of product methyl esters in ester exchange reaction unavoidably with crude glycerine of the byproduct containing methyl alcohol
Discharge, the present invention utilizes density contrast, and methyl esters is overflowed and the circulation of ester exchange reaction device is returned to, and reaction is participated in again, realizes
Closed cycle, it is to avoid the discharge of effluent, it is ensured that the methyl esters of all reactions generations is all recycled, improve product
Rate.Using methyl alcohol and the boiling-point difference of glycerine, crude glycerine is come with separating methanol by methanol rectifying tower, methyl alcohol is the ester in preceding road
Exchange reaction provides raw material, is able to whole recyclings.
As a further improvement on the present invention, the crude glycerine from the discharge of methanol rectification tower bottom is circulated into glycerine drying tower
Dry, thoroughly the crude glycerine of dehydration is pumped back in crude glycerine temporary storage tank, for pre-esterification reactor provides crude glycerine containing soap.The present invention
Using the accessory substance of the system generation for pre-esterification reactor provides crude glycerine containing soap, realize and recycle, make realization of the present invention
The continuous circular flow of its own system, and output higher degree glycerine, substantially increase economic benefit and environmental benefit.
As a further improvement on the present invention, the ester exchange reaction device includes retort and knockout drum, the reaction
In the retort under the agitation of stirrer paddle, the first of generation is reacted by being connected with the bottom of knockout drum communicating pipe in the bottom of tank
Ester and the glycerine dissolved with methyl alcohol carry out initial gross separation due to density contrast in the sedimentation separation area of retort, the larger glycerine position of density
In the bottom of retort, the less methyl esters of the density inner chamber for entering knockout drum from communicating pipe above, part is not completely separated
Glycerine also into the inner chamber of knockout drum proceed separate, due to the disturbance without blade, methyl esters and glycerine in knockout drum
Can well be separated, interface sensor and byproduct discharge pneumatic operated valve are respectively equipped with the bottom of retort and knockout drum
Chain control glycerine phase and the interface of methyl esters phase, realize continuously being discharged from the cone bottom of two tank bodies the accessory substance of reaction generation, methyl esters
Discharged from the top of knockout drum.The ester exchange reaction device makes reaction, separation synchronously carry out respectively, and reaction conversion ratio is high, both protects
Being fully contacted for reactant is demonstrate,proved, the time of byproduct sedimentation separation has been in turn ensure that, has also been gone out with accessory substance by interface sensor
The chain of mouthful pneumatic operated valve makes the glycerine phase will not be too close to byproduct discharge with the interface of methyl esters phase, it is to avoid methyl esters is mixed into glycerine
From byproduct discharge discharge, can be needed from main regulation conversion zone and separated region according to production.
As a further improvement on the present invention, the ester exchange reaction device is provided with two-stage, neutral oil and NaOH and
After methyl alcohol mixing, into first order ester exchange reaction, then proceed to add NaOH and methyl alcohol to carry out second level ester exchange anti-
Should.The time of ester exchange reaction can be shortened using two grades of ester exchanges, the conversion ratio of methyl esters is improved, continuous prodution is realized.
As a further improvement on the present invention, the temperature in pre-esterification reactor tower is 185 ± 5 DEG C, and gauge pressure is -0.06MPa,
The pre-esterification reactor time is more than 3 hours；Evaporating temperature in thin film evaporator is 200 ± 5 DEG C, and gauge pressure is -0.095 MPa；
The temperature of neutral oil ester exchange reaction is 60 ± 2 DEG C.In the state of without catalyst, during the reaction of pure glycerin and free fatty
Between need eight hours, in the case where having soap as catalyst, the esterification speed of feedstock oil and crude glycerine is significantly for the present invention
Degree is improved；Temperature and larger negative pressure in pre-esterification reactor tower cause moisture and small molecular weight impurity during pre-esterification reactor
Discharge, it is ensured that follow-up workshop section can obtain the pure glycerine of comparing；The evaporating temperature of thin film evaporator and bigger negative pressure cause sweet
Oil is evaporated.
As a further improvement on the present invention, the feeding temperature of the methanol rectifying tower is 60 ± 2 DEG C, and tower top temperature is 65
± 2 DEG C, column bottom temperature is 105 ± 2 DEG C, and overhead reflux ratio is 1/3, and bottom of towe reflux ratio is 2/3；It is de- in the glycerine drying tower
Coolant-temperature gage is 100 ± 5 DEG C, and gauge pressure is -0.095 MPa.Under this technological parameter, methyl alcohol and crude glycerine can obtain rapid thorough
Separation.
As a further improvement on the present invention, the gauge pressure of the retort and knockout drum inner chamber is -3~-5 millibars；First
Level ester exchange reaction in methyl alcohol addition be the 15% of neutral weight of oil, 0.3% that NaOH addition is neutral weight of oil, instead
It is 30 minutes between seasonable；Methyl alcohol addition is that the 6% of neutral weight of oil, NaOH addition is in the ester exchange reaction of the second level
The 0.1% of neutral weight of oil, the reaction time is 30 minutes.Retort and knockout drum react under tiny structure, can prevent methyl alcohol etc. from having
Noxious material is leaked, and is conducive to improving the security reacted；The addition of methyl alcohol addition and NaOH can just meet instead
Should the need for, can make to be swift in response, thoroughly.
Brief description of the drawings
The present invention is further detailed explanation with reference to the accompanying drawings and detailed description, accompanying drawing only provide with reference to
Illustrate to use, be not used to the limitation present invention.
Fig. 1 is flow chart of the present invention using the deacidification technique of waste grease production glycerine.
In figure：1. the quenched tank of feedstock oil；1a. raw material oil heaters；2. crude glycerine temporary storage tank；2a. crude glycerine heaters；3.
Pre-esterification reactor tower；4. thin film evaporator；5. neutral oil receiving tank；5a. heat exchangers；6. ester exchange reaction device；6a. reacts
Tank；6a1. ester exchange charging apertures；6a2. retort gaseous phase outlets；6a3. retort byproduct is exported；6a4. communicating pipes；6b. points
From tank；6b1. ester interchanged prods are exported；6b2. knockout drum gaseous phase outlets；6b3. knockout drums byproduct is exported；6c. interfaces sense
Device；6d. byproduct discharge pneumatic operated valves；7. methanol rectifying tower；8. glycerine drying tower；9. vapour liquid separator；10. methyl alcohol temporary storage tank；
11. dealcoholization devices；12. water coolers；B1. raw oil pump；B2. crude glycerine adds pump；B3. it is esterified oil pump；B4. glycerine output
Pump；B5. oil slick pump；B6. neutral oil pump；B7. glycerine methyl alcohol rear pump；B8. ester pump is reclaimed；B9. rectifying column glycerine pump；B10. first
Alcohol adds pump；B11. crude glycerine circulating pump；G1. raw material oil pipe；G2. glycerol tube；G3. oil slick return duct；G4. biodiesel output
Pipe；G5. ester exchange by-product QC；G6. NaOH and methyl alcohol adding tube；G7. crude glycerine circulation pipe；G8. crude glycerine reuse pipe；
H1. static mixer one；H2. static mixer two；H3. static mixer three；N1. steam condenser；N2. glycerine condenser；
N3. methanol condenser；N4. water vapor condenser；P1. water seal tank；P2. glycerine collecting pit；P3. oil partition tank；S1. reaction and negative pressure system
System；S2. glycerine negative pressure system is distilled；S3. tiny structure system；S4. methanol rectification negative pressure system；S5. dehydrating glycerin negative pressure system.
Specific embodiment
As shown in figure 1, the deacidification system of waste grease includes that the quenched tank 1 of feedstock oil, pre-esterification reactor tower 3 and crude glycerine are temporary
Deposit tank 2, the entrance of the quenched tank 1 of feedstock oil is connected with raw material oil pipe G1, the outlet of the quenched tank 1 of feedstock oil by raw oil pump B1 with
The entrance of the H1 of static mixer one is connected, and the outlet of the H1 of static mixer one is connected with the charging aperture of pre-esterification reactor tower 3, thick sweet
The bottom of oily temporary storage tank 2 is connected with the entrance of crude glycerine addition pump B2, and crude glycerine adds outlet and the static mixer one of pump B2
The entrance of H1 is connected, and the quenched tank 1 of feedstock oil and crude glycerine temporary storage tank 2 are respectively equipped with heater.
The gaseous phase outlet at the top of pre-esterification reactor tower 3 is connected by steam condenser N1 with reaction and negative pressure system S1, steam
The leakage fluid dram of condenser N1 is connected with water sealing (sealing water) pipe, and the lower end of water sealing (sealing water) pipe is inserted in the bottom of water seal tank P1.
The outlet at bottom of pre-esterification reactor tower 3 is connected by being esterified oil pump B3 with the charging aperture of thin film evaporator 4, and film steams
The gaseous phase outlet on hair device 4 top is connected with the entrance of vapour liquid separator 9, and the top exit of vapour liquid separator 9 is condensed by glycerine
Device N2 is connected with distillation glycerine negative pressure system S2, and the condensate outlet of glycerine condenser N2 inserts glycerine collecting pit by liquid sealing pipe
In the right half pond of P2, the right half pond bottom of glycerine collecting pit P2 is connected by glycerine rear pump B4 with glycerol tube G2.
The outlet at bottom of vapour liquid separator 9 inserts the left half pond of glycerine collecting pit P2, glycerine collecting pit P2 by liquid sealing pipe
Left half pond bottom be connected with the entrance of the quenched tank 1 of feedstock oil by oil slick pump B5 and oil slick return duct G3.
The outlet at bottom of thin film evaporator 4 is connected with the entrance of neutral oil receiving tank 5, and the outlet of neutral oil receiving tank 5 is led to
Cross neutrality oil pump B6 and water cooler 12 is connected with the entrance of the H2 of static mixer two, the entrance of the H2 of static mixer two is also connected with
There are NaOH and methyl alcohol adding tube G6, the outlet of the H2 of static mixer two and the ester exchange charging aperture of ester exchange reaction device 6
6a1 is connected, and the ester exchange gaseous phase outlet of ester exchange reaction device 6 is connected with tiny structure system S3, the ester of ester exchange reaction device 6
Trade-to product outlet 6b1 is connected with dealcoholization device 11, and the outlet of dealcoholization device 11 is connected with biodiesel efferent duct G4.
The inner chamber of neutral oil receiving tank 5 is provided with heat exchanger 5a, and the outlet of raw oil pump B1 is provided with feedstock oil straight-through valve, former
The entrance of the oily straight-through valve of material is connected with the entrance of heat exchanger 5a, and the outlet of heat exchanger 5a is connected with the outlet of feedstock oil straight-through valve.
The ester exchange byproduct outlet of the bottom of ester exchange reaction device 6 accesses oil partition tank P3 by ester exchange by-product QC G5
Right half pond in, the right half pond bottom of oil partition tank P3 is connected by glycerine methyl alcohol rear pump B7 with the centre entrance of methanol rectifying tower 7,
The top gas phase outlet of methanol rectifying tower 7 is connected by methanol condenser N3 with methanol rectification negative pressure system S4, methanol condenser
The condensate outlet of N3 is connected with the entrance of methyl alcohol temporary storage tank 10, and outlet at bottom and the methanol rectifying tower 7 of methyl alcohol temporary storage tank 10 are pushed up
The refluxing opening in portion is connected.The left half pond bottom of oil partition tank P3 is by reclaiming the inlet duct phase of ester pump B8 and the H2 of static mixer two
Even.
The outlet at bottom of methanol rectifying tower 7 is connected by rectifying column glycerine pump B9 with the upper entrance of glycerine drying tower 8, sweet
The bleeding point at the top of oil drying tower 8 is connected by water vapor condenser N4 with dehydrating glycerin negative pressure system S5；The bottom of glycerine drying tower 8
Portion's outlet is connected with the entrance of crude glycerine circulating pump B11, the outlet of crude glycerine circulating pump B11 pass through crude glycerine circulation pipe G7 with it is sweet
The centre entrance of oil drying tower 8 is connected, and the outlet of crude glycerine circulating pump B11 is by crude glycerine reuse pipe G8 and crude glycerine temporary storage tank
2 entrance is connected.
Ester exchange reaction device 6 includes retort 6a and knockout drum 6b, and the inner chamber of retort 6a is including superposed anti-
Area and the sedimentation separation area positioned at bottom are answered, ester exchange charging aperture 6a1 and retort gaseous phase outlet are provided with the top of retort 6a
The bottom that the bottom of 6a2, retort 6a is provided with the outlet of retort byproduct 6a3, retort 6a passes through communicating pipe 6a4 and knockout drum
The bottom of 6b is interconnected, and the top of knockout drum 6b is provided with knockout drum gaseous phase outlet 6b2 and ester interchanged prod outlet 6b1, separates
The bottom of tank 6b is provided with knockout drum byproduct outlet 6b3.
Ester exchange reaction device 6 is provided with two-stage, the ester interchanged prod outlet 6b1 of previous stage by the H3 of static mixer three with
The ester exchange charging aperture 6a1 of rear stage is connected, the entrance of the H3 of static mixer three also simultaneously with NaOH and methyl alcohol adding tube
G6 is connected.
The present invention produces the deacidification technique of glycerine using waste grease, comprises the following steps：After imurity-removal and moisture
Waste grease enters the quenched tank of feedstock oil, and static mixer one is sent to by raw oil pump after being heated by raw material oil heater 1a, contains
Soap crude glycerine enters crude glycerine temporary storage tank, is pumped toward static mixer from crude glycerine addition after being heated by crude glycerine heater 2a
One, feedstock oil carries out pre-esterification reactor after being sufficiently mixed by static mixer one with crude glycerine into pre-esterification reactor tower, slightly
Glycerine generates glyceride under soap catalytic action with the free-fat acid reaction in feedstock oil, and making the acid value of feedstock oil reduces.
In pre-esterification reactor tower, in the case of anhydrous, crude glycerine under soap catalytic action, with feedstock oil in it is free
Fatty acid response generates glyceride, and course of reaction is：
.Temperature in pre-esterification reactor tower 3 is
185 ± 5 DEG C, gauge pressure is -0.06MPa, and the pre-esterification reactor time is more than 3 hours；In the state of without catalyst, pure glycerin with
Reaction time of free fatty needs eight hours, the present invention in the case where having soap as catalyst, feedstock oil and crude glycerine
Esterification speed increase substantially.The present invention replaces methyl alcohol and raw material using the crude glycerine of base-catalyzed transesterification reaction generation
Free-fat acid reaction in oil, can be down to less than 2 by the feedstock oil of acid value 22, meet wanting for next step alkali esterification exchange
Ask, can be used for the raw material of different acid value scopes, methanol consumption can be saved, reduce steam consumption, reduce sour water discharge, reduction sets
Standby corrosion；Prevent methyl alcohol evaporating, emitting, dripping or leaking of liquid or gas, improve workshop security.Weak base soap in crude glycerine as esterification catalysis
Agent, without addition catalyst in addition；Operation safety and reliability, economic benefit is higher.
During pre-esterification reactor, boiling point goes out less than the moisture and small molecular weight impurity of glycerine from the gas phase of pre-esterification reactor tower
Mouth discharge.Using the boiling point of the boiling point higher than water of glycerine, at 185 ± 5 DEG C, gauge pressure is under -0.06MPa, boiling point is less than glycerine
Moisture and small molecular weight impurity shift to an earlier date is discharged from the gaseous phase outlet of pre-esterification reactor top of tower, it is ensured that follow-up workshop section can be compared
Pure glycerine.
Esterised oil from the discharge of the bottom of pre-esterification reactor tower 3 in esterification oil pump B3 feeding thin film evaporators 4 by being steamed
Evaporate, gaseous substance is separated from the gaseous phase outlet on the top of thin film evaporator 4 into vapour liquid separator 9, glycerin vapor is from vapor-liquid separation
The top exit discharge of device 9, into glycerine condenser N2 condensations, the liquid glycerin that condensation is obtained is inserted glycerine and is received by liquid sealing pipe
Collect the right half pond of pond P2, then sent out through glycerol tube G2 by glycerine rear pump B4, obtain the glycerine that mass fraction is more than 96%, it is thin
Evaporating temperature in film evaporator is 200 ± 5 DEG C, and gauge pressure is -0.095 MPa, and at this temperature and larger negative pressure, glycerine is able to
Evaporation.Glycerine can sell as product of the invention, increase economic efficiency.
Contain a small amount of oil slick in the gaseous substance that thin film evaporator 4 is distilled out, after oil slick is isolated through vapour liquid separator 9,
The left half pond of glycerine collecting pit P2 is entered by liquid sealing pipe from the outlet at bottom of vapour liquid separator 9, is extracted out by oil slick pump B5, through floating
Oil return pipe G3 continues to participate in circulation in returning to the quenched tank 1 of feedstock oil, has prevented the discharge of oil slick, it is to avoid the pollution of environment and after
The cost of continuous treatment, improves the yield of finished product of the present invention and semi-finished product.
After esterised oil evaporates glycerine through thin film evaporator 4, neutral oil enters neutral from the outlet at bottom of thin film evaporator 4
Oily receiving tank 5, through being cooled down indirectly in neutral oil pump B6 feeding water coolers 12, the oil temperature of neutral oil is adjusted to ester exchange reaction
60 ± 2 DEG C of required temperature, subsequently into the entrance of the H2 of static mixer two；NaOH（Catalyst）And methyl alcohol is also into quiet
The entrance of the H2 of state blender two, neutral oil carries out ester exchange after mixing with NaOH and methyl alcohol into ester exchange reaction device 6
Reaction obtains methyl esters, and the i.e. common biodiesel of smart methyl esters is obtained through the dealcoholysis of dealcoholization device 11, and biodiesel is steamed through distilling apparatus
Evaporating can obtain purity smart methyl esters and pitch higher.Tiny structure system S3 keeps tiny structure in ester exchange reaction device 6, prevents
The hazardous material situations such as methyl alcohol, are conducive to improving the security reacted.Biodiesel can sell as product, make tool of the present invention
There is economic benefit very high, purity smart methyl esters and pitch higher can be obtained through distillation, waste grease is obtained efficiently
The trans-utilization of benefit, and very environmentally friendly in production process, the discharge of contamination-free and the generation of corrosive deposit.
The feedstock oil first discharged with the quenched tank 1 of feedstock oil from the neutral oil of the bottom of thin film evaporator 4 discharge passes through heat exchanger
5a carries out indirect heat exchange, then the temperature as needed for the oil temperature of neutral oil is down to ester exchange reaction by water cooler 12, neutral grease
The temperature of exchange reaction is 60 ± 2 DEG C.The neutral oil that thin film evaporator 4 is discharged is cooled down using feedstock oil, is complied with
Temperature needed for ester exchange reaction device, realizes the UTILIZATION OF VESIDUAL HEAT IN of neutral oil, the load of road water cooler 12 after mitigation, while
The temperature of feedstock oil can be improved, the purpose of energy efficiency is reached.
The ester exchange byproduct that generation is reacted in ester exchange reaction device 6 includes crude glycerine and a small amount of methyl esters containing methyl alcohol,
There is minimal amount of product methyl esters to be discharged with crude glycerine of the byproduct containing methyl alcohol in ester exchange reaction unavoidably, into the right side of oil partition tank P3
In half pond after further stratification, methyl esters enters in left half pond from the overfall overflow on oil partition tank P3 tops, mixed by static state
Clutch comes back to ester exchange reaction device 6 and participates in reaction again.The methyl alcohol and glycerine of the right half ponds of oil partition tank P3 are by glycerine methyl alcohol
Rear pump B7 sends into the centre entrance of methanol rectifying tower 7, and methanol steam is discharged from the top of methanol rectifying tower 7, through methanol condensed
Device N3 condensations turn into liquid, and into methyl alcohol temporary storage tank 10, the methyl alcohol that methyl alcohol temporary storage tank 10 is reclaimed is partly into methanol rectifying tower 7
The refluxing opening at top.The lower part outlet of methyl alcohol temporary storage tank 10 adds pump B10 and NaOH and methyl alcohol adding tube G6 by methyl alcohol
It is connected.Methyl alcohol another part that methyl alcohol temporary storage tank 10 is reclaimed is sent by methyl alcohol addition pump B10 through NaOH and methyl alcohol adding tube G6
Enter in ester exchange reaction device 6, ester exchange reaction device 6 is come from the byproduct of itself ester exchange reaction using methyl alcohol, it is real
Existing closed cycle, reduce the consumption of material, it is to avoid the discharge of noxious material.
The feeding temperature of methanol rectifying tower is 60 ± 2 DEG C, and tower top temperature is 65 ± 2 DEG C, and column bottom temperature is 105 ± 2 DEG C, tower
Top reflux ratio is 1/3, and bottom of towe reflux ratio is 2/3, and the gauge pressure of methanol rectifying tower inner chamber is -3~-5 millibars.In this technological parameter
Under, methyl alcohol and crude glycerine can obtain thoroughly separating rapidly.
Ester exchange reaction device 6 produce reaction by-product methyl alcohol and glycerine after the rectifying of methanol rectifying tower 7, crude glycerine from
The outlet at bottom discharge of methanol rectifying tower 7, through the upper entrance of crude glycerine circulating pump B11 feeding glycerine drying tower 8, crude glycerine exists
Circulated in glycerine drying tower 8 in the presence of crude glycerine circulating pump B11, the dehydration temperaturre in glycerine drying tower is 100 ± 5 DEG C,
Gauge pressure is -0.095 MPa, is dehydrated in the presence of dehydrating glycerin negative pressure system S5, and water vapour is taken out from the top of glycerine drying tower 8
Gas port is discharged, and is condensed into liquid by water vapor condenser N4, and enter water seal tank P1.Through the crude glycerine of thorough dehydration through thick sweet
Oily reuse pipe G8 is returned in crude glycerine temporary storage tank 2, for pre-esterification reactor provides crude glycerine containing soap.The present invention is produced using the system
Accessory substance provide crude glycerine containing soap for pre-esterification reactor, realize and recycle, the present invention is realized the company of its own system
Continuous circular flow, and output higher degree glycerine, substantially increase economic benefit and environmental benefit.
In the retort 6a under the agitation of stirrer paddle, the glycerine of product methyl esters and byproduct dissolved with methyl alcohol of generation is reacted
Initial gross separation is carried out in the sedimentation separation area of retort 6a, the larger glycerine of density is located at lower section can be from anti-because density is different
Answer tank byproduct export 6a3 discharge, the less methyl esters of density it is above from retort connected entrance by communicating pipe 6a4 enter point
From the inner chamber of tank 6b, the glycerine that part is not completely separated proceeds to separate also into the inner chamber of knockout drum 6b；In knockout drum 6b
In can be separated well due to the disturbance without blade, methyl esters and glycerine, react the by-product glycerin of generation from two tanks
The cone bottom discharge of body.Interface sensor 6c and byproduct discharge pneumatic operated valve are respectively equipped with the bottom of retort 6a and knockout drum 6b
6d chain control glycerine phases and the interface of methyl esters phase, realize the accessory substance of continuous discharge reaction generation.Methyl esters is final from knockout drum
The ester interchanged prod outlet 6b1 discharges on 6b tops, glycerine exports 6a3 and knockout drum byproduct outlet 6b3 from retort byproduct
Discharge.
The ester exchange reaction device 6 makes reaction, separation synchronously carry out respectively, and reaction conversion ratio is high, both ensure that reactant
Be fully contacted, in turn ensure that the time of byproduct sedimentation separation.The gauge pressure of retort and knockout drum inner chamber is -3~-5 millibars,
The hazardous material situations such as methyl alcohol are prevented, is conducive to improving the security reacted.Also by interface sensor and byproduct discharge gas
The chain of dynamic valve makes the glycerine phase will not be too close to byproduct discharge with the interface of methyl esters phase, it is to avoid methyl esters is mixed into glycerine from pair
Product exit is discharged, and can be needed from main regulation conversion zone and separated region according to production.
Ester exchange reaction device is provided with two-stage, after neutral oil mixes with NaOH and methyl alcohol, into first order ester exchange
Reaction, then proceeding to addition NaOH and methyl alcohol carries out second level ester exchange reaction.Can shorten ester using two grades of ester exchanges
The time of exchange reaction, the conversion ratio of methyl esters is improved, realize continuous prodution.
Methyl alcohol addition is that the 15% of neutral weight of oil, NaOH addition is neutral oil in first order ester exchange reaction
The 0.3% of weight, the reaction time is 30 minutes；Methyl alcohol addition is the 6% of neutral weight of oil, hydrogen-oxygen in the ester exchange reaction of the second level
It is the 0.1% of neutral weight of oil to change sodium addition, and the reaction time is 30 minutes.The addition of methyl alcohol addition and NaOH can
The need for just to meet reaction, can make to be swift in response, thoroughly.
The foregoing is only the preferable possible embodiments of the present invention, non-therefore limitation patent protection model of the invention
Enclose.In addition to the implementation, the present invention can also have other embodiment.The skill that all use equivalents or equivalent transformation are formed
Art scheme, all falls within the protection domain of application claims.Technical characteristic of the present invention without description can be by or using now
There is technology to realize, will not be repeated here.
Claims (13)
1. a kind of utilization waste grease produces the deacidification technique of glycerine, comprises the following steps：It is discarded after imurity-removal and moisture
Grease enters the quenched tank of feedstock oil, and static mixer one is sent to by raw oil pump after being heated, it is characterised in that：Crude glycerine containing soap
Into crude glycerine temporary storage tank, from crude glycerine addition pumping toward static mixer one after being heated, feedstock oil is with crude glycerine by quiet
State blender one carries out pre-esterification reactor after being sufficiently mixed into pre-esterification reactor tower, crude glycerine under soap catalytic action, with original
Free-fat acid reaction generation glyceride in material oil, making the acid value of feedstock oil reduces.
2. a kind of utilization waste grease according to claim 1 produces the deacidification technique of glycerine, it is characterised in that：It is described pre-
In esterification reaction process, boiling point is arranged less than the moisture and small molecular weight impurity of glycerine from the gaseous phase outlet of the pre-esterification reactor tower
Go out.
3. a kind of utilization waste grease according to claim 1 produces the deacidification technique of glycerine, it is characterised in that：Pre-esterification
Into being distilled in thin film evaporator, the gaseous substance that thin film evaporator is evaporated is into vapour-liquid point for the glyceride that obtains of reaction
From device separate, from vapour liquid separator top discharge glycerin vapor through glycerine condenser condense after obtain mass fraction for 96% with
On glycerine.
4. a kind of utilization waste grease according to claim 3 produces the deacidification technique of glycerine, it is characterised in that：From vapour-liquid
The oil slick of separator bottom discharge continues to participate in circulation in returning to the quenched tank of feedstock oil.
5. a kind of utilization waste grease according to claim 3 produces the deacidification technique of glycerine, it is characterised in that：From described
After the neutral oil cooling of thin film evaporator bottom discharge, NaOH and methyl alcohol are added, it is common after mixing through static mixer two
Ester exchange reaction being carried out into ester exchange reaction device and obtaining containing alcohol methyl esters, containing alcohol methyl esters obtains biodiesel through dealcoholysis.
6. a kind of utilization waste grease according to claim 5 produces the deacidification technique of glycerine, it is characterised in that：From described
Feedstock oil of the neutral oil of thin film evaporator bottom discharge first with the quenched tank discharge of feedstock oil carries out indirect heat exchange by heat exchanger,
Temperature as needed for water cooler adjusts to ester exchange reaction the oil temperature of neutral oil again.
7. a kind of utilization waste grease according to claim 5 produces the deacidification technique of glycerine, it is characterised in that：The ester
The ester exchange byproduct of exchange reaction bottom of device discharge includes crude glycerine and a small amount of methyl esters containing methyl alcohol, is stood into oil partition tank
After layering, the methyl esters overflowed from upper strata returns to the circulation of ester exchange reaction device, and crude glycerine of the oil partition tank bottom containing methyl alcohol is admitted to
The centre entrance of methanol rectifying tower, methanol steam is extracted from the top of methanol rectifying tower, and liquid is turned into through methanol condenser condensation
State, into methyl alcohol temporary storage tank, the methyl alcohol that methyl alcohol temporary storage tank is reclaimed is partly into the refluxing opening of methanol rectification top of tower, another portion
Divide and return to circulation in the ester exchange reaction device, crude glycerine is discharged from the bottom of methanol rectifying tower.
8. a kind of utilization waste grease according to claim 7 produces the deacidification technique of glycerine, it is characterised in that：From methyl alcohol
The crude glycerine of rectifier bottoms discharge enters glycerine drying tower cyclic drying, and it is temporary that the crude glycerine being thoroughly dehydrated is pumped back to crude glycerine
In depositing tank, for pre-esterification reactor provides crude glycerine containing soap.
9. a kind of utilization waste grease according to claim 5 produces the deacidification technique of glycerine, it is characterised in that：The ester
Exchange reaction device include retort and knockout drum, the bottom of the retort by being connected with the bottom of knockout drum communicating pipe,
In the retort under the agitation of stirrer paddle, react generation methyl esters and dissolved with methyl alcohol glycerine because density contrast is in retort
Sedimentation separation area carries out initial gross separation, and the larger glycerine of density is located at the bottom of retort, and the less methyl esters of density is above
Enter the inner chamber of knockout drum from communicating pipe, the glycerine that part is not completely separated proceeds to separate also into the inner chamber of knockout drum,
Due to the disturbance without blade in knockout drum, methyl esters and glycerine can be separated well, in retort and knockout drum
Bottom is respectively equipped with interface sensor and byproduct discharge pneumatic operated valve chain control glycerine phase and the interface of methyl esters phase, realizes from two
The accessory substance of reaction generation is continuously discharged at the cone bottom of tank body, and methyl esters is discharged from the top of knockout drum.
10. a kind of utilization waste grease according to claim 9 produces the deacidification technique of glycerine, it is characterised in that：It is described
Ester exchange reaction device is provided with two-stage, after neutral oil mixes with NaOH and methyl alcohol, into first order ester exchange reaction, then
Continuously adding NaOH and methyl alcohol carries out second level ester exchange reaction.
A kind of 11. utilization waste greases according to claim 5 produce the deacidification technique of glycerine, it is characterised in that：Pre- ester
It is 185 ± 5 DEG C to change the temperature in reaction tower, and gauge pressure is -0.06MPa, and the pre-esterification reactor time is more than 3 hours；Thin film evaporation
Evaporating temperature in device is 200 ± 5 DEG C, and gauge pressure is -0.095 MPa；The temperature of neutral oil ester exchange reaction is 60 ± 2 DEG C.
A kind of 12. utilization waste greases according to claim 8 produce the deacidification technique of glycerine, it is characterised in that：It is described
The feeding temperature of methanol rectifying tower is 60 ± 2 DEG C, and tower top temperature is 65 ± 2 DEG C, and column bottom temperature is 105 ± 2 DEG C, overhead reflux ratio
It is 1/3, bottom of towe reflux ratio is 2/3；Dehydration temperaturre in the glycerine drying tower is 100 ± 5 DEG C, and gauge pressure is -0.095 MPa.
A kind of 13. utilization waste greases according to claim 10 produce the deacidification technique of glycerine, it is characterised in that：It is described
The gauge pressure of retort and knockout drum inner chamber is -3~-5 millibars；Methyl alcohol addition is neutral weight of oil in first order ester exchange reaction
15%, 0.3% that NaOH addition is neutral weight of oil, the reaction time be 30 minutes；First in the ester exchange reaction of the second level
Alcohol addition is the 6% of neutral weight of oil, NaOH addition is neutral weight of oil 0.1%, the reaction time is 30 minutes.
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