CN206799570U - A kind of deacidification system of waste grease - Google Patents
A kind of deacidification system of waste grease Download PDFInfo
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- CN206799570U CN206799570U CN201720324284.9U CN201720324284U CN206799570U CN 206799570 U CN206799570 U CN 206799570U CN 201720324284 U CN201720324284 U CN 201720324284U CN 206799570 U CN206799570 U CN 206799570U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/74—Recovery of fats, fatty oils, fatty acids or other fatty substances, e.g. lanolin or waxes
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Abstract
It the utility model is related to a kind of deacidification system of waste grease, including the quenched tank of feedstock oil, crude glycerine temporary storage tank and pre-esterification reactor tower, the entrance of the quenched tank of feedstock oil is connected with raw material oil pipe, the outlet of the quenched tank of feedstock oil is connected by raw oil pump, static mixer with the charging aperture of pre-esterification reactor tower, the bottom of crude glycerine temporary storage tank is added pump by crude glycerine and is connected with the entrance of static mixer, and the quenched tank of feedstock oil and crude glycerine temporary storage tank are respectively equipped with heater.The outlet at bottom of pre-esterification reactor tower is connected by being esterified oil pump with the charging aperture of thin film evaporator, the gaseous phase outlet of thin film evaporator is connected with vapour liquid separator, the top exit of vapour liquid separator is connected by glycerine condenser with negative pressure system, the condensate outlet of glycerine condenser is inserted in glycerine collecting pit by liquid sealing pipe, and the bottom of glycerine collecting pit is connected by glycerine rear pump with glycerol tube.The system can reduce corrosion and reduce sour water and produce, be more environmentally friendly, saving and reducing production cost.
Description
Technical field
A kind of deacidification system of waste grease is the utility model is related to, belongs to grease processing technology field.
Background technology
As people are increasingly reduced and the concern increasingly of environmental pollution to non-renewable energy resources, waste resource comprehensive utilization,
Develop the raw material of industry of the friendly recyclable fuel of novel environmental or high value as current scientific research hot subject it
One.By waste grease be converted into diesel oil substitute fuel have the advantages that it is renewable and biodegradable, to mitigate atmospheric greenhouse
Gas concentration, the living environment for improving the mankind, realize that economic sustainable development has great importance.China has greatly every year
The waste grease of amount, make full use of this quasi-grease that there is very high economic value, can solve gutter oil again and flow to dining table, threaten
The safe diet of people.But because this kind of acid value of oil and fat is high, impurity is more, complicated component, it 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 and given birth to using soda acid two-step method
Thing diesel oil, add sulfuric acid catalysis（Or other solid acids）, it is passed through excessive methanol and carries out pre-esterification with the free fatty in raw material
Reaction, reaction is promoted to be carried out to positive direction to reduce the acid value of raw material and take away the moisture of generation, after pre-esterification is fully reacted,
Sodium hydroxide is added, methanol, carries out ester exchange reaction, standing separation goes out by-product glycerin after reacting completely, after isolating glycerine,
Dealcoholysis, washing and drying, rectifying must refine methyl esters respectively.
Existing deacidification technique two：Raw material after pretreatment, using the method for physical deacidification, remove free in raw material
After aliphatic acid, sodium hydroxide is added, methanol, carries out ester exchange reaction, dealcoholysis after reacting completely, and to go out accessory substance sweet for standing separation
After oil, washing and drying, rectifying must refine methyl esters.Free fatty through depickling generation is with methanol 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, high is required to equipment material, it is serious to corrosive pipeline, produce acid
Water causes environmental pollution, and processing is difficult, high using solid catalyst cost, and 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, poisonous, inflammable, the easy leakage of methanol steam, is unfavorable for operating personnel's
It is healthy and high to the requirement of workshop electrical equipment explosive-proof grade.Phase transformation consumed energy during methanol gasifying, contain after excessive methanol is condensed
Water needs rectifying more, need to consume higher energy, increases rectifying load and needs 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, and the cost that equipment is put into for the first time is high.
Utility model content
The purpose of this utility model is, overcomes problems of the prior art, there is provided a kind of deacidification of waste grease
System, it is possible to reduce the corrosion to equipment, reduce the generation of sour water, make more environmentally friendly technique, energy-conservation and reduce production cost.
It is quenched to solve above technical problem, a kind of deacidification system of waste grease of the present utility model, including feedstock oil
Tank, pre-esterification reactor tower and crude glycerine temporary storage tank, the entrance of the quenched tank of feedstock oil are connected with raw material oil pipe, the feedstock oil
The outlet of quenched tank is connected by raw oil pump with the entrance of static mixer one, the outlet of the static mixer one with it is described
The charging aperture of pre-esterification reactor tower is connected, and the bottom of the crude glycerine temporary storage tank is connected with the entrance of crude glycerine addition pump, described
The outlet of crude glycerine addition pump is connected with the entrance of the static mixer one, and the quenched tank of feedstock oil and the crude glycerine are temporary
Deposit tank and be respectively equipped with heater.
Relative to prior art, the utility model achieves following beneficial effect：Abandoned oil after imurity-removal and moisture
Fat enters the quenched tank of feedstock oil by raw material oil pipe, and static mixer one is sent to by raw oil pump after being heated；Come from alkali to urge
The crude glycerine containing soap for changing ester exchange reaction generation enters crude glycerine temporary storage tank, and static state is also directed to by crude glycerine addition pump after being heated
Blender one, feedstock oil enters pre-esterification reactor tower after being sufficiently mixed with crude glycerine by static mixer one, anti-in pre-esterification
Ying Tazhong, in the case of anhydrous, crude glycerine generates glycerine under soap catalytic action, with the free-fat acid reaction in feedstock oil
Ester, course of reaction are：
。
The utility model replaces methanol and the free fatty in feedstock oil using the crude glycerine of base-catalyzed transesterification reaction generation
Reaction, can be down to less than 2 by the feedstock oil of acid value 22, meet the requirement that the esterification of next step alkali exchanges, available for different acid values
The raw material of scope, methanol consumption can be saved, reduce steam consumption, reduced sour water discharge, reduce equipment corrosion；Prevent methanol
Evaporating, emitting, dripping or leaking of liquid or gas, the security for improving workshop.Catalyst of the weak base soap as esterification in crude glycerine, urged without addition in addition
Agent；Safety and reliability is operated, economic benefit is higher.
As improvement of the present utility model, the gaseous phase outlet of the pre-esterification reactor top of tower by steam condenser with it is anti-
Negative pressure system is answered to be connected, the leakage fluid dram of the steam condenser is connected with water sealing (sealing water) pipe, and the lower end of the water sealing (sealing water) pipe is inserted in water seal
The bottom in pond.It is higher than the boiling point of water using the boiling point of glycerine, the temperature and negative pressure in pre-esterification reactor tower cause boiling point less than sweet
The moisture and small molecular weight impurity of oil shift to an earlier date discharges from the gaseous phase outlet of pre-esterification reactor top of tower, ensures that follow-up workshop section can obtain
Purer glycerine.
As further improvement of the utility model, the outlet at bottom of the pre-esterification reactor tower by be esterified oil pump with it is thin
The charging aperture of film evaporator is connected, and the gaseous phase outlet on the thin film evaporator top is connected with the entrance of vapour liquid separator, described
The top exit of vapour liquid separator is connected by glycerine condenser with distillation glycerine negative pressure system, the condensation of the glycerine condenser
Liquid outlet is inserted by liquid sealing pipe in the right half pond of glycerine collecting pit, and the right half pond bottom of the glycerine collecting pit is defeated by glycerine
Go out pump with glycerol tube to be connected.It is pumped into thin film evaporator and is carried out by esterised oil from the esterised oil of pre-esterification reactor tower bottom discharge
Distillation, glycerin vapor enter vapour liquid separator separation from the gaseous phase outlet on thin film evaporator top, and glycerin vapor is from vapor-liquid separation
The top exit discharge of device, is condensed into glycerine condenser, and the liquid glycerin for condensing to obtain is inserted glycerine by liquid sealing pipe and collected
The right half pond in pond, then sent out by glycerine rear pump through glycerol tube, the glycerine that mass fraction is more than 96% is obtained, glycerine can be made
Sell for product of the present utility model, increase economic efficiency.
As further improvement of the utility model, described in the outlet at bottom of the vapour liquid separator is inserted by liquid sealing pipe
The left half pond of glycerine collecting pit, the left half pond bottom of the glycerine collecting pit pass through oil slick pump and oil slick return duct and the raw material
The entrance of the quenched tank of oil is connected.Contain a small amount of liquid oil slick in the gaseous substance that thin film evaporator distills out, liquid oil slick is by vapour
After liquid/gas separator is isolated, the left half pond of glycerine collecting pit is discharged into by liquid sealing pipe from the outlet at bottom of vapour liquid separator, is floated
Oil pump is extracted out, is returned to through oil slick return duct in the quenched tank of feedstock oil and is continued to participate in circulation, prevented the discharge of oil slick, avoided environment
Pollution and subsequent treatment cost, improve the yield of the utility model finished product and semi-finished product.
As further improvement of the utility model, the outlet at bottom of the thin film evaporator and entering for neutral oil receiving tank
Mouth is connected, and the outlet of the neutral oil receiving tank is connected by neutral oil pump and water cooler with the entrance of static mixer two,
The entrance of the static mixer two is also associated with sodium hydroxide and methanol adding tube, the outlet of the static mixer two and ester
The ester exchange charging aperture of exchange reaction device is connected, ester exchange gaseous phase outlet and the tiny structure system of the ester exchange reaction device
It is connected, the ester interchanged prod outlet of the ester exchange reaction device is connected with dealcoholization device, the outlet and life of the dealcoholization device
Thing diesel oil efferent duct is connected.Esterised oil is after thin film evaporator evaporates glycerine, outlet at bottom of the neutral oil from thin film evaporator
Kept in into neutral oil receiving tank, be pumped into water cooler through neutral oil and cool down indirectly, the oil temperature of neutral oil is adjusted to ester
Temperature needed for exchange reaction, subsequently into the entrance of static mixer two；Sodium hydroxide and methanol also enter static mixer
Two entrance, neutral oil enter ester exchange reaction device progress ester exchange reaction and obtain containing alcohol after being mixed with sodium hydroxide and methanol
Methyl esters, the i.e. generally described biodiesel of smart methyl esters is obtained through dealcoholization device dealcoholysis, biodiesel can be with through distilling apparatus distillation
Obtain purity higher smart methyl esters and pitch.Tiny structure is kept in ester exchange reaction device, prevents the hazardous material situations such as methanol,
Be advantageous to improve the security of reaction.
As further improvement of the utility model, the inner chamber of the neutral oil receiving tank is provided with heat exchanger, the raw material
The outlet of oil pump is provided with feedstock oil straight-through valve, and the entrance of the feedstock oil straight-through valve is connected with the entrance of the heat exchanger, institute
The outlet for stating heat exchanger is connected with the outlet of the feedstock oil straight-through valve.The neutral oil discharged using feedstock oil to thin film evaporator
Cooled down, comply with the temperature needed for ester exchange reaction device, realize the UTILIZATION OF VESIDUAL HEAT IN of neutral oil, road oil temperature after mitigation
The load of cooling, while the temperature of feedstock oil can be improved, reach the purpose of energy efficiency.
As further improvement of the utility model, the ester exchange byproduct outlet of the ester exchange reaction bottom of device is logical
Cross in the right half pond of ester exchange by-product QC access oil partition tank, the right half pond bottom of the oil partition tank passes through glycerine methanol rear pump
It is connected with methanol rectifying tower centre entrance, the top gas phase outlet of the methanol rectifying tower passes through methanol condenser and methanol rectification
Negative pressure system is connected, and the condensate outlet of the methanol condenser is connected with the entrance of methanol temporary storage tank, the methanol temporary storage tank
Outlet at bottom be connected with the refluxing opening of the methanol rectification top of tower.Ester exchange pair caused by reaction in ester exchange reaction device
Product includes crude glycerine containing methanol and a small amount of methyl esters, into the right half pond of oil partition tank after further stratification, methyl esters from
The overfall overflow on oil partition tank top enters in left half pond, and methanol and glycerine are pumped into methanol rectifying tower by the output of glycerine methanol
Centre entrance, methanol steam are discharged from the top of methanol rectifying tower, are turned into liquid through methanol condenser condensation, are kept in into methanol
Tank, the methanol of methanol temporary storage tank recovery are partly into the refluxing opening of methanol rectification top of tower.
As further improvement of the utility model, the lower part outlet of the methanol temporary storage tank adds pump and institute by methanol
State sodium hydroxide and methanol adding tube is connected.Methanol another part of methanol temporary storage tank recovery adds pump through sodium hydroxide by methanol
And methanol adding tube is sent into ester exchange reaction device, ester exchange reaction device is come from itself ester exchange reaction using methanol
Byproduct, realize closed cycle, reduce the consumption of material, avoid the discharge of noxious material.
As further improvement of the utility model, the left half pond bottom of the oil partition tank by reclaim ester pump with it is described quiet
The inlet duct of state blender two is connected.Overflow enters the methyl esters of the left half pond of oil partition tank after stratification, passes through static mixer
Come back to ester exchange reaction device to participate in reacting again, realize closed cycle, both avoided the discharge of reaction product, carried again
The high yield of biodiesel.
As further improvement of the utility model, the outlet at bottom of the methanol rectifying tower by rectifying column glycerine pump with
The upper entrance of glycerine drying tower is connected, and the bleeding point at the top of the glycerine drying tower is born by water vapor condenser and dehydrating glycerin
Pressure system is connected；The outlet at bottom of the glycerine drying tower is connected with the entrance of crude glycerine circulating pump, the crude glycerine circulating pump
Outlet be connected by crude glycerine circulation pipe with the centre entrance of the glycerine drying tower, the outlet of the crude glycerine circulating pump leads to
The entrance that crude glycerine reuse pipe is crossed with the crude glycerine temporary storage tank is connected.Reaction by-product methanol caused by ester exchange reaction device
With glycerine after methanol rectifying tower rectifying, crude glycerine is discharged from the outlet at bottom of methanol rectifying tower, is pumped into through crude glycerine circulation
The upper entrance of glycerine drying tower, crude glycerine are circulated in glycerine drying tower in the presence of crude glycerine circulating pump, taken off in glycerine
It is dehydrated in the presence of water negative pressure system, water vapour is cold by its by water vapor condenser from the bleeding point discharge at the top of glycerine drying tower
Coagulate for liquid, and be discharged into water seal tank；Crude glycerine through being thoroughly dehydrated is returned in crude glycerine temporary storage tank through crude glycerine reuse pipe, is pre-
Esterification provides crude glycerine containing soap, realizes and recycles, and the utility model is realized using the byproduct of itself
Continuous circular flow, and the glycerine of output higher degree, substantially increase economic benefit and environmental benefit.
Brief description of the drawings
The utility model is described in further detail with reference to the accompanying drawings and detailed description, accompanying drawing only provides ginseng
Examine and used with explanation, be not used to limit the utility model.
Fig. 1 is the flow chart of the deacidification system of the utility model waste grease.
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 exports；6a4. communicating pipe；6b. points
From tank；6b1. ester interchanged prods export；6b2. knockout drum gaseous phase outlets；6b3. knockout drums byproduct exports；6c. interfaces sense
Device；6d. byproduct discharge pneumatic operated valves；7. methanol rectifying tower；8. glycerine drying tower；9. vapour liquid separator；10. methanol temporary storage tank；
11. dealcoholization device；12. water cooler；B1. raw oil pump；B2. crude glycerine addition pump；B3. it is esterified oil pump；B4. glycerine exports
Pump；B5. oil slick pump；B6. neutral oil pump；B7. glycerine methanol 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 exports
Pipe；G5. ester exchange by-product QC；G6. sodium hydroxide and methanol 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.
Embodiment
As shown in figure 1, the deacidification system of the utility model waste grease includes the quenched tank 1 of feedstock oil, pre-esterification reactor tower 3
With crude glycerine temporary storage tank 2, the entrance of the quenched tank 1 of feedstock oil is connected with raw material oil pipe G1, and the outlet of the quenched tank 1 of feedstock oil passes through original
Material oil pump B1 is connected with the H1 of static mixer one entrance, the H1 of static mixer one outlet and the charging of pre-esterification reactor tower 3
Mouthful be connected, the bottom of crude glycerine temporary storage tank 2 is connected with crude glycerine addition pump B2 entrance, crude glycerine add pump B2 outlet with it is quiet
The H1 of state blender one entrance is connected, and the quenched tank 1 of feedstock oil and crude glycerine temporary storage tank 2 are respectively equipped with heater.
Waste grease enters the quenched tank 1 of feedstock oil by raw material oil pipe G1, by raw material after being heated by raw material oil heater 1a
Oil pump B1 is sent to the H1 of static mixer one；The crude glycerine containing soap for coming from base-catalyzed transesterification reaction generation is kept in into crude glycerine
Tank 2, the H1 of static mixer one, feedstock oil and crude glycerine are also directed to by crude glycerine addition pump B2 after being heated by crude glycerine heater 2a
Enter pre-esterification reactor tower 3 after being sufficiently mixed by the H1 of static mixer one, in pre-esterification reactor tower 3, crude glycerine is urged in soap
Under change effect, glyceride is generated with the free-fat acid reaction in feedstock oil, course of reaction is：
。
Temperature in pre-esterification reactor tower 3 is 185 ± 5 DEG C, and gauge pressure is -0.06MPa, and the pre-esterification reactor time is more than 3 hours.
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
Condenser N1 leakage fluid dram is connected with water sealing (sealing water) pipe, and the lower end of water sealing (sealing water) pipe is inserted in water seal tank P1 bottom.Utilize the boiling point of glycerine
Higher than the boiling point of water, temperature and negative pressure in pre-esterification reactor tower 3 cause boiling point to be carried less than the moisture and small molecular weight impurity of glycerine
The preceding gaseous phase outlet discharge from the top of pre-esterification reactor tower 3, ensure that follow-up workshop section can obtain purer glycerine.
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 glycerine condenser N2 condensate outlet inserts glycerine collecting pit by liquid sealing pipe
In P2 right half pond, glycerine collecting pit P2 right half pond bottom is connected by glycerine rear pump B4 with glycerol tube G2.
It is sent into thin film evaporator 4 and is distilled by esterification oil pump B3 from the esterised oil of the bottom of pre-esterification reactor tower 3 discharge,
Gaseous substance separates from the gaseous phase outlet on the top of thin film evaporator 4 into vapour liquid separator 9, and glycerin vapor is from vapour liquid separator 9
Top exit discharge, condensed into glycerine condenser N2, condense obtained liquid glycerin and pass through liquid sealing pipe and insert glycerine to collect
Pond P2 right half pond, then sent out by glycerine rear pump B4 through glycerol tube G2, obtain the glycerine that mass fraction is more than 96%, glycerine
It can sell as product of the present utility model, increase economic efficiency.Evaporating temperature in thin film evaporator is 200 ± 5
DEG C, gauge pressure is -0.095 MPa；The temperature of neutral oil ester exchange reaction is 60 ± 2 DEG C.
The outlet at bottom of vapour liquid separator 9 inserts glycerine collecting pit P2 left half pond, glycerine collecting pit P2 by liquid sealing pipe
Left half pond bottom be connected by the entrance of oil slick pump B5 and oil slick return duct G3 tanks 1 quenched with feedstock oil.Thin film evaporator 4 steams
Contain a small amount of oil slick in the gaseous substance distillated, oil slick goes out after vapour liquid separator 9 is isolated from the bottom of vapour liquid separator 9
Mouth is discharged into glycerine collecting pit P2 left half pond by liquid sealing pipe, is extracted out by oil slick pump B5, feedstock oil is returned to through oil slick return duct G3
Circulation is continued to participate in quenched tank 1, has prevented the discharge of oil slick, the pollution of environment and the cost of subsequent treatment is avoided, improves
The yield of the utility model finished product and semi-finished product.
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 leads to
Cross neutral oil pump B6 and water cooler 12 with the H2 of static mixer two entrance to be connected, the H2 of static mixer two entrance is also connected with
There are sodium hydroxide and methanol adding tube G6, the H2 of static mixer two outlet 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.
After thin film evaporator 4 evaporates glycerine, neutral oil enters neutral esterised oil from the outlet at bottom of thin film evaporator 4
Oily receiving tank 5, it is sent into water cooler 12 through neutral oil pump B6 and cools down indirectly, the oil temperature of neutral oil is adjusted to ester exchange reaction
60 ± 2 DEG C of required temperature, subsequently into the H2 of static mixer two entrance；Catalyst and methanol also enter static mixer two
H2 entrance, neutral oil enter the progress of ester exchange reaction device 6 ester exchange reaction and obtain containing alcohol after being mixed with catalyst and methanol
Methyl esters, the i.e. common biodiesel of smart methyl esters is obtained through the dealcoholysis of dealcoholization device 11, biodiesel can obtain through distilling apparatus distillation
The smart methyl esters and pitch higher to purity.Tiny structure is kept in ester exchange reaction device 6, prevents the hazardous material situations such as methanol,
Be advantageous to improve the security of reaction, gaseous substance caused by ester exchange is extracted out by tiny structure system S3.
The inner chamber of neutral oil receiving tank 5 is provided with heat exchanger 5a, and raw oil pump B1 outlet is provided with feedstock oil straight-through valve, former
Expect that the entrance of oily straight-through valve is connected with heat exchanger 5a entrance, heat exchanger 5a outlet is connected with the outlet of feedstock oil straight-through valve.
The neutral oil discharged using feedstock oil to thin film evaporator 4 is cooled down, and complies with the temperature needed for ester exchange reaction device 6
Degree, the UTILIZATION OF VESIDUAL HEAT IN of neutral oil is realized, the load that road oil temperature cools down after mitigation, while the temperature of feedstock oil can be improved, make
The effect of pre-esterification reactor is more preferable, reaches the purpose of energy efficiency.
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, oil partition tank P3 right half pond bottom is connected by glycerine methanol 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
N3 condensate outlet is connected with the entrance of methanol temporary storage tank 10, and outlet at bottom and the methanol rectifying tower 7 of methanol temporary storage tank 10 push up
The refluxing opening in portion is connected.
Ester exchange byproduct includes the crude glycerine containing methanol and a small amount of methyl esters caused by reaction in ester exchange reaction device 6,
Into in oil partition tank P3 right half pond after further stratification, methyl esters enters left half from the overfall overflow on oil partition tank P3 tops
Chi Zhong, methanol and glycerine are sent into the centre entrance of methanol rectifying tower 7 by glycerine methanol rear pump B7, and methanol steam is from methanol rectification
The top discharge of tower 7, turn into liquid through methanol condenser N3 condensations, into methanol temporary storage tank 10, the recovery of methanol temporary storage tank 10
Methanol is partly into the refluxing opening at the top of methanol rectifying tower 7.The feeding temperature of methanol rectifying tower 7 is 60 ± 2 DEG C, tower top temperature
For 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, methanol rectifying tower inner chamber
Gauge pressure is -3~-5 millibars.The lower part outlet of methanol temporary storage tank 10 adds pump B10 by methanol and added with sodium hydroxide and methanol
Pipe G6 is connected.Methanol another part that methanol temporary storage tank 10 reclaims adds pump B10 through sodium hydroxide and methanol adding tube by methanol
G6 is sent into ester exchange reaction device 6, ester exchange reaction device 6 is come from the by-product of itself ester exchange reaction using methanol
Product, closed cycle is realized, reduce the consumption of material, avoid the discharge of noxious material.
Oil partition tank P3 left half pond bottom is connected by reclaiming ester pump B8 with the H2 of static mixer two inlet duct.Stand
Overflow enters the methyl esters of the left half ponds of oil partition tank P3 after layering, and ester exchange reaction device 6 is come back to again by static mixer
Reaction is participated in, closed cycle is realized, has both avoided the discharge of reaction product, improve the yield of biodiesel again.
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 outlet is connected with crude glycerine circulating pump B11 entrance, crude glycerine circulating pump B11 outlet by crude glycerine circulation pipe G7 with it is sweet
The centre entrance of oil drying tower 8 is connected, and crude glycerine circulating pump B11 outlet passes through crude glycerine reuse pipe G8 and crude glycerine temporary storage tank
2 entrance is connected.
Reaction by-product methanol caused by ester exchange reaction device 6 and glycerine after the rectifying of methanol rectifying tower 7, crude glycerine from
The outlet at bottom discharge of methanol rectifying tower 7, the upper entrance of glycerine drying tower 8 is sent into through crude glycerine circulating pump B11, and crude glycerine exists
Circulate in glycerine drying tower 8 in the presence of crude glycerine circulating pump B11, be dehydrated in the presence of dehydrating glycerin negative pressure system S5,
Water vapour is condensed into liquid, and be discharged into water seal tank from the bleeding point discharge at the top of glycerine drying tower 8 by water vapor condenser N4
P1；Dehydration temperaturre in glycerine drying tower is 100 ± 5 DEG C, and gauge pressure is -0.095 MPa.Crude glycerine through being thoroughly dehydrated is through thick sweet
Oily reuse pipe G8 is returned in crude glycerine temporary storage tank 2, is provided crude glycerine containing soap for pre-esterification reactor, is realized and recycle, and makes this
Utility model can realize continuous circular flow, and the glycerine of output higher degree using the byproduct of itself, greatly improve
Economic benefit and environmental benefit.
Ester exchange reaction device 6 includes retort 6a and knockout drum 6b, and retort 6a inner chamber is including superposed anti-
Answer area and be provided with ester exchange charging aperture 6a1 and retort gaseous phase outlet positioned at the sedimentation separation area of bottom, retort 6a top
6a2, retort 6a bottom are provided with retort byproduct outlet 6a3, and retort 6a bottom passes through communicating pipe 6a4 and knockout drum
6b bottom is interconnected, and knockout drum 6b top is provided with knockout drum gaseous phase outlet 6b2 and ester interchanged prod outlet 6b1, separation
Tank 6b bottom is provided with knockout drum byproduct outlet 6b3.
In retort 6a under the agitation of stirrer paddle, react generation product methyl esters and byproduct dissolved with methanol glycerine
Because density difference in retort 6a sedimentation separation area carries out initial gross separation, the larger glycerine of density is located at lower section can be from anti-
Tank byproduct outlet 6a3 discharges are answered, the less methyl esters of density is above to pass through the entrance point of communicating pipe 6a4 from retort connected entrance
From tank 6b inner chamber, the glycerine that part is not completely separated also continues to separate into knockout drum 6b inner chamber；In knockout drum 6b
In can be separated well due to the disturbance of no 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 retort 6a and knockout drum 6b bottom
The interface of 6d chain control glycerine phases and methyl esters phase, realize the accessory substance of continuous discharge reaction generation.Methyl esters is finally from knockout drum
The ester interchanged prod outlet 6b1 discharges on 6b tops, glycerine export 6a3 and knockout drum byproduct outlet 6b3 from retort byproduct
Discharge.The ester exchange reaction device 6 makes reaction, separation are synchronous respectively to carry out, and reaction conversion ratio is high, both ensure that filling for reactant
Tap is touched, and in turn ensure that the time of byproduct sedimentation separation.Retort and the gauge pressure of knockout drum inner chamber are -3~-5 millibars, are prevented
The hazardous material situations such as methanol, be advantageous to improve the security of reaction.
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 H3 of static mixer three entrance also simultaneously with sodium hydroxide and methanol adding tube
G6 is connected.After first order ester exchange reaction, catalyst and methanol are continuously added, second level ester exchange reaction is carried out, can make
Ester exchange reaction is more thorough, and first order ester exchange reaction can also be made rapider.Methanol adds in first order ester exchange reaction
Dosage is the 15% of neutral weight of oil, sodium hydroxide addition is neutral weight of oil 0.3%, reaction time are 30 minutes；Second
Level ester exchange reaction in methanol addition be the 6% of neutral weight of oil, 0.1% that sodium hydroxide addition is neutral weight of oil, instead
It is 30 minutes between seasonable.
It the foregoing is only the preferable possible embodiments of the utility model, non-therefore limitation patent of the present utility model
Protection domain.In addition to the implementation, the utility model can also have other embodiment.It is all to use equivalent substitution or equivalent change
The technical scheme to be formed is changed, is all fallen within the protection domain of the requires of the utility model.Technology of the utility model without description is special
Sign can be realized by or using prior art, will not be repeated here.
Claims (10)
1. a kind of deacidification system of waste grease, including the quenched tank of feedstock oil and pre-esterification reactor tower, the quenched tank of feedstock oil
Entrance be connected with raw material oil pipe, the outlet of the quenched tank of feedstock oil passes through the entrance phase of raw oil pump and static mixer one
Even, the outlet of the static mixer one is connected with the charging aperture of the pre-esterification reactor tower, it is characterised in that：Also include thick sweet
Oily temporary storage tank, the bottom of the crude glycerine temporary storage tank are connected with the entrance of crude glycerine addition pump, and the crude glycerine addition pump goes out
Mouth is connected with the entrance of the static mixer one, and the quenched tank of feedstock oil and the crude glycerine temporary storage tank are respectively equipped with heating
Device.
2. the deacidification system of waste grease according to claim 1, it is characterised in that：The pre-esterification reactor top of tower
Gaseous phase outlet is connected by steam condenser with reaction and negative pressure system, and the leakage fluid dram of the steam condenser is connected with water sealing (sealing water) pipe,
The lower end of the water sealing (sealing water) pipe is inserted in the bottom of water seal tank.
3. the deacidification system of waste grease according to claim 1, it is characterised in that：The bottom of the pre-esterification reactor tower
Outlet is connected by being esterified oil pump with the charging aperture of thin film evaporator, gaseous phase outlet and the vapour-liquid point on the thin film evaporator top
Entrance from device is connected, and the top exit of the vapour liquid separator is connected by glycerine condenser with distillation glycerine negative pressure system,
The condensate outlet of the glycerine condenser is inserted by liquid sealing pipe in the right half pond of glycerine collecting pit, the glycerine collecting pit
Right half pond bottom is connected by glycerine rear pump with glycerol tube.
4. the deacidification system of waste grease according to claim 3, it is characterised in that：The bottom of the vapour liquid separator goes out
Mouth inserts the left half pond of the glycerine collecting pit by liquid sealing pipe, the left half pond bottom of the glycerine collecting pit by oil slick pump and
Oil slick return duct is connected with the entrance of the quenched tank of the feedstock oil.
5. the deacidification system of waste grease according to claim 3, it is characterised in that：The bottom of the thin film evaporator goes out
Mouth is connected with the entrance of neutral oil receiving tank, and the outlet of the neutral oil receiving tank passes through neutral oil pump and water cooler and static state
The entrance of blender two is connected, and the entrance of the static mixer two is also associated with sodium hydroxide and methanol adding tube, described quiet
The outlet of state blender two is connected with the ester exchange charging aperture of ester exchange reaction device, the ester exchange of the ester exchange reaction device
Gaseous phase outlet is connected with tiny structure system, and the ester interchanged prod outlet of the ester exchange reaction device is connected with dealcoholization device, institute
The outlet for stating dealcoholization device is connected with biodiesel efferent duct.
6. the deacidification system of waste grease according to claim 5, it is characterised in that：The inner chamber of the neutral oil receiving tank
Provided with heat exchanger, the outlet of the raw oil pump is provided with feedstock oil straight-through valve, the entrance of the feedstock oil straight-through valve with it is described
The entrance of heat exchanger is connected, and the outlet of the heat exchanger is connected with the outlet of the feedstock oil straight-through valve.
7. the deacidification system of waste grease according to claim 5, it is characterised in that：The ester exchange reaction bottom of device
Ester exchange byproduct outlet by ester exchange by-product QC access oil partition tank right half pond in, under the right half pond of the oil partition tank
Portion is connected by glycerine methanol rear pump with methanol rectifying tower centre entrance, and the top gas phase outlet of the methanol rectifying tower passes through
Methanol condenser is connected with methanol rectification negative pressure system, the condensate outlet of the methanol condenser and the entrance of methanol temporary storage tank
It is connected, the outlet at bottom of the methanol temporary storage tank is connected with the refluxing opening of the methanol rectification top of tower.
8. the deacidification system of waste grease according to claim 7, it is characterised in that：The bottom of the methanol temporary storage tank goes out
Mouth adds pump by methanol and is connected with the sodium hydroxide and methanol adding tube.
9. the deacidification system of waste grease according to claim 7, it is characterised in that：The left half pond bottom of the oil partition tank
It is connected by reclaiming ester pump with the inlet duct of the static mixer two.
10. the deacidification system of waste grease according to claim 7, it is characterised in that：The bottom of the methanol rectifying tower
Outlet is connected by rectifying column glycerine pump with the upper entrance of glycerine drying tower, and the bleeding point at the top of the glycerine drying tower passes through
Water vapor condenser is connected with dehydrating glycerin negative pressure system；The outlet at bottom of the glycerine drying tower and the entrance of crude glycerine circulating pump
It is connected, the outlet of the crude glycerine circulating pump is connected by crude glycerine circulation pipe with the centre entrance of the glycerine drying tower, institute
The outlet for stating crude glycerine circulating pump is connected by crude glycerine reuse pipe with the entrance of the crude glycerine temporary storage tank.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201720324284.9U CN206799570U (en) | 2017-03-30 | 2017-03-30 | A kind of deacidification system of waste grease |
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| CN201720324284.9U CN206799570U (en) | 2017-03-30 | 2017-03-30 | A kind of deacidification system of waste grease |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106929163A (en) * | 2017-03-30 | 2017-07-07 | 迈安德集团有限公司 | A kind of deacidification system of waste grease |
| CN113563977A (en) * | 2021-07-21 | 2021-10-29 | 湖北天基生物能源科技发展有限公司 | Waste grease treatment system and treatment method |
-
2017
- 2017-03-30 CN CN201720324284.9U patent/CN206799570U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106929163A (en) * | 2017-03-30 | 2017-07-07 | 迈安德集团有限公司 | A kind of deacidification system of waste grease |
| CN106929163B (en) * | 2017-03-30 | 2023-03-28 | 迈安德集团有限公司 | Acid reducing system for waste oil |
| CN113563977A (en) * | 2021-07-21 | 2021-10-29 | 湖北天基生物能源科技发展有限公司 | Waste grease treatment system and treatment method |
| CN113563977B (en) * | 2021-07-21 | 2022-08-16 | 湖北天基生物能源科技发展有限公司 | Treatment system and treatment method for waste grease |
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