CN108395937A - A kind of method and system producing biodiesel - Google Patents
A kind of method and system producing biodiesel Download PDFInfo
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- CN108395937A CN108395937A CN201710066669.4A CN201710066669A CN108395937A CN 108395937 A CN108395937 A CN 108395937A CN 201710066669 A CN201710066669 A CN 201710066669A CN 108395937 A CN108395937 A CN 108395937A
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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
-
- 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, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
-
- 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
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- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of method and system producing biodiesel, this method includes following content：（1）Raw oil material and alcohols are added to certain proportion in premixing tank and premixed；（2）Liquid phase material after premix is passed through air and liquid mixer with gas, carries out gas-liquid mixed；（3）Gas-liquid mixed material is passed through in the horizontal blending tank of mixing reactor and carries out esterification；Wherein, horizontal blending tank does reciprocating linear motion in the horizontal direction under the action of reciprocator；（4）Esterification reaction product flows through ejector and enters products pot, after the partial reaction product reflux to ejector in products pot, passes through ejector and comes back in products pot.The present invention enhances the stability of system, and can long-term continuous operation under the premise of keeping a wide range of efficiently mixing mass-transfer performance.
Description
Technical field
The invention belongs to technical field of biodiesel preparation, are related to a kind of method and system producing biodiesel.
Background technology
Biodiesel is also known as biodiesel, is the cleaning produced as raw material using renewable biological sources such as animal and plant greases
Fuel, physics and chemical property are very close even better with petrifaction diesel.Biodiesel be a kind of Novel pollution-free can
The renewable sources of energy, have many advantages, such as to be easy to that degradation, burning pollutant discharge is low, greenhouse gas emission is few.In industrialized production, generally
It is produced using chemical method, i.e., is raw material with animal or plant grease, with the low-carbon alcohols such as methanol or ethyl alcohol in acid or base catalysis
Agent effect is lower to carry out ester exchange reaction, and biodiesel is prepared.The reactor of traditional mode of production biodiesel mostly uses machinery and stirs
Reactor is mixed, industrial common reactor is the intermittent autoclave stirred reactor with stirring facility, and this reactor lacks
Point is that back-mixing is uneven, and stirring efficiency is not high, and is unsuitable for operating continuously.To solve this problem, it is proposed that a kind of novel
Reactor-impact flow reactor increases material contact area since material mutually clashes in reactor, makes heat transfer, mass transfer
Rate accordingly increases, and promotes carrying out for the chemical reaction influenced by mass transport process.
CN201046396Y discloses a kind of irrotationality vertical circulation impact flow reactor, is set in reactor there are two water conservancy diversion
Cylinder is correspondingly provided with propeller in each guide shell, and the hand of spiral of the propeller is on the contrary, be respectively used to push fluid from charging
Mouth is flowed through guide shell to fluid impingement zone, and contact area is increased by high-speed impact, to reach the mesh for strengthening mass transfer
's.But since fluid is invariably prone to stream line motion, contacting with each other between divided fluid is difficult, therefore impingement region
Strengthening mixing has certain limit.And vibrations or the bearing sealing failure of propeller and arbor are easily caused, lead to mechanical breakdown.
CN1814344A discloses one kind and being used for liquid reactive impact flow reactor, and two are mounted among the reactor
One or two pumps are arranged outside in guide shell, reactor, and the outlet of pump is symmetrically arranged on the feed side of guide shell, and reaction mass is through pump
Conveying is hit in opposite directions through guide shell flow at high speed and at center, effectively promotes the mixing of reaction mass.The reactor makes
Structure design is simplified instead of the structure of propeller type with pumped type outer circulation percussion flow, cost is reduced, reduces simultaneously
Caused by propeller type structure the problems such as vibrations, bearing sealing failure.But above-mentioned reactor center regional fluid speed is larger, and all
Side fluid velocity is small, and mixing nor very uniformly, using pumped type Circulative impinging stream, external Mechanical Driven being needed largely to flow in addition
Body high speed clashes, and energy consumption is larger.
CN1952048A discloses a kind of production method of biodiesel, and for this method in impact flow reactor, material is logical
Cross guide shell to move to middle part, and hit in opposite directions at this, striking face and around formed impingement region.After shock, fluid passes through
Ring casing between guide shell and container inner wall returns to the left and right ends of container respectively, is then divided into and does not pass through left and right two by charging conveying
A guide shell flow direction middle part is simultaneously hit again, is recycled repeatedly, achieve the purpose that it is uniformly mixed, it is fast to improve mass transfer
Rate.But the above method also uses pumped type Circulative impinging stream, needs a large amount of fluid high-speeds head-on collision of external Mechanical Driven, energy consumption compared with
Greatly.
Invention content
In view of the deficienciess of the prior art, the present invention provides a kind of method and system producing biodiesel, this method
Under the premise of keeping a wide range of efficiently mixing mass-transfer performance, the stability of system is enhanced, and can long-term continuous operation.
The method of the production biodiesel of the present invention, including following content：
（1）Raw oil material and alcohols are added to certain proportion in premixing tank and premixed；
（2）Liquid phase material after premix is passed through air and liquid mixer with gas, carries out gas-liquid mixed；
（3）Gas-liquid mixed material is passed through in the horizontal blending tank of mixing reactor and carries out esterification；Wherein, horizontal blending tank
It does reciprocating linear motion in the horizontal direction under the action of reciprocator；
（4）Esterification reaction product flows through ejector and enters products pot, after the partial reaction product reflux to ejector in products pot,
Ejector is passed through to come back in products pot.
In the method for the present invention, step（1）The grease and alcohols is made a living the common raw material of generation diesel oil.Grease uses
Animal and plant grease, the grease with 10 ~ 18 carbon atoms in preferred fat acid group；Alcohols uses low with 1 ~ 8 carbon atom
Molecular weight monohydric alcohol, preferably methanol or ethyl alcohol.The molar ratio of the grease and alcohols is 3：1~10：1, preferably 4：1~8：1.In advance
The catalyst such as the KOH and/or NaOH that are generally added during mixed, catalyst charge are the 0.1% ~ 1% of raw material total amount, premix temperature
Degree is 20 ~ 130 DEG C, and it is 0.1 ~ 0.5 hour to do time in advance, and the premixing tank is the common blending tank of industry.
In the method for the present invention, step（2）The gas is one or more of helium, neon, argon gas or nitrogen；Gas
The ratio between the volume flow of body and the total volumetric flow rate of liquid phase material are 1：5~1：20, preferably 1：8~1：15.The gas-liquid mixed
The common blending tank of industry may be used in device, and gas is passed through from mixing pot bottom, and is arranged at gas feed in blending tank and is bubbled
Device, bubbler are immersed in grease with alcohols, and gas after the aperture effusion in bubbler by, by being bubbled agitated liquid, promoting gas
Liquid mixes；The air and liquid mixer can also use the air and liquid mixer based on venturi principle, such as ejector gas-liquid to mix
Clutch.
In the method for the present invention, step（3）The esterification condition is：Reaction temperature be 30 ~ 130 DEG C, preferably 50 ~
120 DEG C, the reaction time is 0.5 ~ 6 hour.Horizontal blending tank, which is carried out continuously, first to be accelerated to slow down afterwards, reversed again first accelerates to slow down afterwards
The reciprocal change speed linear motion of periodical high-frequency rate, the frequency of reciprocating motion are generally 5 ~ 1000 times/second, preferably 10-600 times/
Second.The fill factor of horizontal blending tank is 0.6 ~ 0.8, wherein the fill factor is liquid volume and blending tank in blending tank
The ratio between volume.
In the method for the present invention, step（4）In, effect of the liquid through pump to flow back in products pot enters ejector, and passes through
Ejector nozzle at high speeds sprays, and the kinetic energy formed using high-velocity fluid generates negative pressure in the throat of ejector, thus by reactor
The liquid of outflow sucks ejector, and phegma and the liquid of reactor outflow carry out mixing jetting in the diffuser pipe of ejector, then
Into in products pot, the gas in products pot is then flowed out from gas vent, and comes back to gas feed to recycle.Step
（4）Described in ejector can also use the other types of mixer based on venturi principle.
Mixing reactor described in the method for the present invention, including horizontal blending tank, feed hose, discharge tube and reciprocal fortune
Dynamic device；The both ends of horizontal blending tank are respectively set inlet port and outlet port, one end of feed hose connect horizontal blending tank into
Material mouth, other end connection charging, one end of discharge tube connect the discharge port of horizontal blending tank, other end connection discharging；Back and forth
Telecontrol equipment includes two parallel guide rails, spring, sliding block or wheel, pedestal II, fixed seat, driving device and sliding rack；Its
Middle sliding rack includes pedestal I and connecting plate；Two parallel guide rails are horizontal positioned, and fixed seat is symmetrically fixed on two guide rails or so
The inside at both ends（I.e. a fixed seat is fixed in every guide rail left and right ends）, connected by spring between fixed seat and pedestal II
It connects；Sliding rack and 4 fixed seats are in same plane, for the vertical guide rail direction of the left and right sides 2 pedestal I and be parallel to guide rail
Two connecting plates constitute rectangular configuration；Wherein pedestal I is strip, and length is slightly less than the spacing of two closed slides, even
Installation sliding block or wheel below fishplate bar, sliding block or wheel are equipped with groove, and rail crown is equipped with longitudinal ridge along its length, guide rail
Longitudinal ridge is engaged with the groove of sliding block or wheel；Horizontal blending tank is fixed on the sliding rack of reciprocator, driving device
It is connected with pedestal I or pedestal II；Deflector can be set inside horizontal blending tank.
Wherein, feed hose and the material of discharge tube are determined according to material properties, and rubber hose, plastics generally can be used
Hose, corrugated flexible hose and metal hose etc..Hose has certain length, ensures that hose begins in blending tank reciprocatory movement
There is certain slackness eventually, in order to avoid hose is caused to damage or leaked with blending tank and material import and export junction.Wherein
Feed inlet is preferably placed at discharge port on same level axis.
In the mixing reactor of the present invention, horizontal blending tank end socket can be ellipse, butterfly, taper, spherical or flat
Cover head.
In the mixing reactor of the present invention, the volume of horizontal blending tank is depending on actual conditions.Liquid is equipped in blending tank
Level detecting apparatus controls charging or discharge velocity by level sensing, maintains the liquid level in blending tank.
In the mixing reactor of the present invention, sliding block or the contact surface of wheel and guide rail are equipped with groove, and rail crown is along length
Direction is equipped with longitudinal ridge, and the longitudinal ridge of guide rail is engaged with the groove of sliding block or wheel, ensures sliding block or wheel in driving device
It moves along a straight line along rail length direction under effect.
In the mixing reactor of the present invention, sliding block or wheel are arranged symmetrically, and number is at least 2 pairs, preferably 2-4 pairs.Sliding block
Can be welded between connecting plate can also be threadedly coupled；Each pair of wheel is fixedly connected with a horizontal axis, between axis and connecting plate
It is connected through bearing.
In the mixing reactor of the present invention, guide rail will have certain guiding accuracy, movement to answer light steady；There is foot
Enough rigidity, to bear outer load.Guide rail should also have good wearability, guide rail in use, wear extent should be made smaller,
And can compensate or be conveniently adjusted automatically after wearing, the contact surface for sliding or rolling between guide rail and sliding block or wheel answers enough light
It is sliding, reduce frictional resistance.
In the mixing reactor of the present invention, the spring between connect base and fixed seat has enough rigidity and stiffness system
Number, depending on diameter, spring diameter, spring pitch and the spring material of spring steel wire are according to specific actual conditions.
In the mixing reactor of the present invention, the spacing of the longitudinal ridge of two closed slides is the 1.1-1.5 of blending tank diameter
Times, preferably 1.2-1.4 times, the both ends of guide rail are concordant with fixed seat outer end or slightly above fixed seat outer end.
In the mixing reactor of the present invention, horizontal blending tank is fixedly connected with two pieces of connecting plates of sliding rack.It can will connect
Fishplate bar is welded with blending tank；Or protrusion is set on connecting plate, blending tank is blocked；Can also on blending tank weld pad plate, then
Backing plate and connecting plate are bolted.
In the mixing reactor of the present invention, the reciprocating motion of the ranging from sliding rack between the fixed seat of guide rail left and right ends is empty
Between；Horizontal blending tank on sliding rack is linear reciprocating motion, pedestal I and pedestal II along guide rail between the fixed seat of left and right ends
It periodically collides and contacts in reciprocatory movement.
In the mixing reactor of the present invention, connecting plate length preferably mixes canister length slightly larger than mixing canister length
1.1-1.2 again.
In the mixing reactor of the present invention, the distance between fixed seat of same root guide rail left and right ends is not less than and fixation
1.1 times, preferably 1.1-1.3 times of the corresponding pedestal I spacing of seat.
In the mixing reactor of the present invention, driving device can use electronic, pneumatic, hydraulic-driven or magnetic drive etc.；
When using electronic, pneumatic and hydraulic-driven, driving device is connect with pedestal I 4-3, pedestal I4-3 is acted on, when using magnetic force
When driving, driving device is preferably connected with pedestal II 4-6, by continuous reverse drive or transformation pole orientation, make blending tank into
The reciprocal change speed linear motion of row.
Under driving device effect, blending tank carries out the reciprocal change speed linear motion in left and right.It is horizontal under driving device effect
Blending tank carries out reciprocal change speed linear motion；First, horizontal blending tank moves under driving force effect to the even acceleration in side, the side
Pedestal I contacted with the pedestal II on guide rail after, spring between pedestal II and fixed seat constantly generates flexible deformation by compression,
The kinetic energy of horizontal blending tank is converted into the elastic potential energy of spring；As spring is gradually compressed, horizontal blending tank is in spring force
Under effect, the speed of horizontal blending tank movement constantly reduces, until the speed of horizontal blending tank reduces to zero；Then, horizontal mixing
Tank accelerates under the side driving force and by the elastic force effect of compressed spring to the other side, as the pedestal I and guide rail of the other side
On pedestal II when just contacting, horizontal blending tank reaches maximum speed, with the constantly quilt of the spring between pedestal II and fixed seat
Compression, under the action of spring power, horizontal blending tank reduces speed now movement, and the speed of horizontal blending tank reduces to zero again；
Blending tank changes the direction of motion again under the action of driving force and spring force, and the horizontal such cyclic movement of blending tank makes
Constantly all directions are mutually hit at various locations between material and reactor wall, mixed material in tank, promote material mixed
It closes, strengthens material mass transfer, improve the reaction efficiency between material.
The mixing reactor of the present invention drives horizontal blending tank progress high-frequent reciprocating speed change straight by reciprocator
Line moves, and in movement section, blending tank is first accelerated under the action of driving device, and in the work of spring power
Blending tank is set to be gradually decrease to zero, then the reversed periodical high-frequency rate for accelerating, slowing down by compression process medium velocity in spring under
Reciprocal change speed linear motion.In blending tank motion process, the speed of blending tank or increase or reduce, the speed of any time
It is all changing, also blending tank plays progress variable motion to the gas-liquid mixture in blending tank therewith.Due to material itself in tank
Inertia force effect, mixed material with mix between top tank structure and continuous all directions phase at various locations between mixed material
It mutually hits, avoids the presence in dead zone.Material into horizontal blending tank is in preliminary gas-liquid mixture phase, by horizontal blending tank
High-frequency reciprocating change speed linear motion after, further promote gas-liquid mixed, so that whole materials is formd uniformly mixed gas-liquid mixed
Object is closed, the contact area of grease and alcohols is increased, enhances the microcosmic back-mixing effect of reactor, grease can reach with alcohols
The other mixed effect of molecular level is strengthened mass transfer and is reacted, material is made to mix on a large scale to realize between grease and alcohols
Each position all directions are all able to be sufficiently mixed and react in tank, accelerate reaction rate, substantially reduce the reaction time, carry
High mass transfer and production efficiency.Simultaneously because spring also acts the effect of buffering so that blending tank and reciprocator
Impact force is smaller, is conducive to the even running of device.Using intermittent operation and continous way operation can stable operation, it is preferential to select
It is operated with continous way.Overcome that the only main impingement region mixing situation of common impact flow reactor at present is good, the mixing of other regions is weaker
The shortcomings that and impact flow reactor be unsuitable for continuous operation the shortcomings that, can efficiently be run with long-term smooth.
The present invention production biodiesel system, include mainly：Premixing tank, air and liquid mixer, mixing reactor, jet stream
Device, pump and products pot；Grease feed inlet, alcohols feed inlet and premix material outlet is arranged in premixing tank；Air and liquid mixer is equipped with liquid
Phase import, gas phase import and the outlet of gas-liquid mixed material；Mixing reactor includes horizontal blending tank, feed hose, discharge tube
And reciprocator；Material inlet, refluxing opening, outlet for product and gas vent is arranged in products pot；The pre-composition of premixing tank
Material outlet is connected through the fluid inlet of pipeline and air and liquid mixer, the gas-liquid mixed material outlet of air and liquid mixer and hybrid reaction
The feed hose of device connects, and the discharge tube of mixing reactor connect with ejector feed entrance, ejector export through pipeline and
Products pot import connects, and product pot bottom is exported equipped with phegma, and phegma outlet is connect through pipeline with ejector reflux inlet,
Gas is returned again to gas phase import and is recycled after the outflow of the gas vent of products pot.
Reactor of the present invention using above-mentioned mixing reactor as production biodiesel, is passed through into reactor through gas-liquid
The gas-liquid mixed material tentatively mixed after mixer effect is being reacted by the high-frequency reciprocating change speed linear motion of reactor
Large-scale impingement region is formed in device so that the gas-liquid mixed material tentatively mixed further mixes, and then makes whole material shapes
At uniformly mixed gas-liquid mixture, the contact area of raw oil material and alcohols is increased, makes the grease in reactor and alcohols
It is sufficiently mixed, reaches the other mixed effect of molecular level, greatly enhance microcosmic mixing and microcosmic mass transfer, what is relatively mitigated
Under reaction condition, reaction rate is accelerated, shortens the reaction time, improves mass transfer and production efficiency.Present system structure
Simply, it is easily installed and safeguards, and simplify technological process, reduce production cost and capital cost of reactor, nothing in production process
Discharging of waste liquid is an environmentally protective process.
Description of the drawings
Fig. 1 is the schematic diagram of the production biodiesel system of the present invention.
Fig. 2 is the front view of the mixing reactor in the present invention.
Fig. 3 is the vertical view of the mixing reactor in the present invention.
Wherein 8- greases feed inlet；9- alcohols feed inlets；10- premixing tanks；11- ejectors；12- products pots；13- is pumped；14-
Outlet for product；15- mixing reactors；16- gas vents；17- air and liquid mixers；18- bubblers；19- gas phase imports；
Mixing reactor includes：1- reactor feeds；2- reactor feed hoses；The horizontal blending tanks of 3-；4- reciprocators；
5- reactor discharge tubes；6- reactors discharge；7- liquid level detection devices；
Reciprocator 4 includes：4-1- guide rails, 4-2- springs, 4-3- pedestal I, 4-4- connecting plate, 4-5- sliding blocks or wheel,
4-6- pedestal II, 4-7- fixed seat, 4-8- driving devices, 4-9- sliding racks.
Specific implementation mode
The method and system of the production biodiesel of the present invention are illustrated below in conjunction with the accompanying drawings.
The present invention production biodiesel system, include mainly：Premixing tank 10, air and liquid mixer 17, mixing reactor
15, ejector 11, pump 13 and products pot 12.Grease feed inlet 8, alcohols feed inlet 9 and premix material outlet is arranged in premixing tank 10；
Air and liquid mixer 17 is equipped with fluid inlet, gas phase import 19 and the outlet of gas-liquid mixed material；Mixing reactor 15 includes horizontal mixed
Close tank 3, feed hose 2, discharge tube 5 and reciprocator 4；Material inlet, refluxing opening, product discharge is arranged in products pot 12
Mouth 14 and gas vent 16.The premix material outlet of premixing tank 12 connects through the premix material inlet of pipeline and air and liquid mixer 17
It connects, the gas-liquid mixed material outlet of air and liquid mixer 17 is connect with the feed hose 2 of mixing reactor 15, mixing reactor 15
Discharge tube 5 is connect with 11 feed entrance of ejector, and the outlet of ejector 11 is connect through pipeline with 12 import of products pot, products pot 12
Bottom is exported equipped with phegma, and phegma outlet is connect through pipeline with 11 reflux inlet of ejector, gas of the gas from products pot 12
After 16 outflow of body outlet, returns again to gas phase import 19 and recycle.
The system of the production biodiesel of the present invention is run as follows：
Raw oil material and alcohols with certain proportion respectively by grease feed inlet 8 and alcohols feed inlet 9 be added in premixing tank 10 into
Row premix；Grease after preliminary premix is passed through air and liquid mixer 17, simultaneously by raw oil material with after alcohols tentatively premix with alcohols
Gas is passed into certain proportion in air and liquid mixer 17, gas is made fully to carry out gas-liquid mixed with liquid phase material；It will be preliminary
Feed hose 2 of the mixed gas-liquid material through mixing reactor 15, which enters, carries out esterification in horizontal blending tank 3, wherein horizontal
Blending tank 3 does reciprocating linear motion under the action of reciprocator 4；Esterification reaction product flows through ejector 11 and enters product
Tank 12, the partial reaction product in products pot 12 are sprayed after pump 13 is back to ejector 11 by 11 nozzle at high speeds of ejector,
The kinetic energy formed using high-velocity fluid generates negative pressure in the throat of ejector 11, and the liquid sucking that mixing reactor 15 flows out is penetrated
Stream device 11 simultaneously comes back to products pot 12；Gas in products pot 12 flows out from gas vent 16 and comes back to gas feed 19
To recycle.
Embodiment 1
Using soybean oil and methanol as raw material, the molar ratio of soybean oil and methanol is 6：1, catalyst use KOH, content be only into
Expect the 0.1% of total amount.Soybean oil, methanol and catalyst are passed through in premixing tank, the soybean oil after premix is passed through gas-liquid with methanol
In blending tank, while nitrogen is passed through into gas-liquid mixed tank, the volume flow of nitrogen and the total volumetric flow rate of grease and alcohols it
Than being 1：12.Raw soybeans oil and methanol and gas are passed through after tentatively being mixed in air and liquid mixer in mixing reactor.Mixing
The displacement that reactor moves back and forth is 2 times of reactor length, and reciprocating frequency is 200 times/second, and the reaction time is
The fill factor of 1h, horizontal blending tank are 0.8, and feed rate and discharge velocity are mix tank volume 1/20.From products pot
The reaction product of outlet conduit outflow obtains aliphatic ester phase by standing separation（Upper layer）, utilize the 6890N of agilent company
Chromatographic measures fatty acid triglycercide high conversion rate up to 95.7%.
Embodiment 2
Using palm oil and methanol as raw material, the molar ratio of palm oil and methanol is 6：1, catalyst use KOH, content be only into
Expect the 0.1% of total amount.Palm oil, methanol and catalyst are passed through in premixing tank, by after premix palm oil and methanol be passed through gas-liquid
In blending tank, while helium is passed through into gas-liquid mixed tank, the volume flow of helium and the total volumetric flow rate of grease and alcohols it
Than being 1：12.Raw material palm oil and methanol and gas are passed through after tentatively being mixed in air and liquid mixer in mixing reactor, are mixed
The displacement that reactor moves back and forth is 2 times of reactor length, and reciprocating frequency is 200 times/second, and the reaction time is
The fill factor of 1h, horizontal blending tank are 0.8, and feed rate and discharge velocity are mix tank volume 1/20.From products pot
The reaction product of outlet conduit outflow obtains aliphatic ester phase by standing separation（Upper layer）, utilize the 6890N of agilent company
Chromatographic measures fatty acid triglycercide high conversion rate up to 96.3%.
Embodiment 3
As described in Example 1, the displacement that mixing reactor moves back and forth is still 2 times of reactor length, only back and forth
Motion frequency is 300 times/second.The reaction product flowed out from products pot outlet conduit obtains aliphatic ester phase by standing separation
（Upper layer）, using the 6890N chromatographics of agilent company, fatty acid triglycercide high conversion rate is measured up to 98.2%.
Embodiment 4
As described in Example 1, only the ratio between the volume flow of nitrogen and the total volumetric flow rate of grease and alcohols are 1：10.From production
The reaction product of product tank outlet conduit outflow obtains aliphatic ester phase by standing separation（Upper layer）, utilize agilent company
6890N chromatographics measure fatty acid triglycercide high conversion rate up to 99.1%.
Comparative example 1
CN1952048A discloses a kind of production method of biodiesel, using methanol and cottonseed oil as the original of production biodiesel
The molar ratio of material, methanol and cottonseed oil is 10：1（Catalyst content is 1.0% or less feed gross mass）, methanol and cottonseed oil
Feed rate be equal to impinging stream reaction volume（I.e. feed volume air speed is 1h-1Namely the reaction time is 1h）.Methanol and cottonseed
After oil premixes in pans, impact flow reactor is squeezed by pump, ester exchange reaction is occurred by shock, circulated material quantity is
The 95% of inlet amount.The reaction product flowed out from static mixer discharge port obtains aliphatic ester phase by standing separation（On
Layer）, using chromatographic, it is 100% to measure fatty acid triglycercide conversion ratio, the content of methyl esters in aliphatic ester phase
It is 91.1%.
Claims (13)
1. a kind of method producing biodiesel, it is characterised in that including following content：（1）By raw oil material and alcohols with certain
Ratio is added in premixing tank and is premixed；（2）Liquid phase material after premix is passed through air and liquid mixer with gas, and it is mixed to carry out gas-liquid
It closes；The gas is one or more of helium, neon, argon gas or nitrogen；（3）It is anti-that gas-liquid mixed material is passed through mixing
It answers and carries out esterification in the horizontal blending tank of device；Wherein, horizontal blending tank under the action of reciprocator along level side
To doing reciprocating linear motion；（4）Esterification reaction product flows through ejector and enters products pot, and the partial reaction product in products pot returns
After flowing to ejector, passes through ejector and come back in products pot.
2. according to the method for claim 1, it is characterised in that：Step（1）The molar ratio of the grease and alcohols is 3：1
~10：1, premix temperature is 20 ~ 130 DEG C, and it is 0.1 ~ 0.5 hour to do time in advance.
3. according to the method for claim 1, it is characterised in that：Step（2）The volume flow and liquid phase object of the gas
The ratio between total volumetric flow rate of material is 1：5~1：20.
4. according to the method for claim 1, it is characterised in that：Step（3）The esterification condition is：Reaction temperature
It it is 30 ~ 130 DEG C, the reaction time is 0.5 ~ 6 hour.
5. according to the method for claim 1, it is characterised in that：Step（3）The horizontal blending tank, which is carried out continuously, first to be added
Slow down after speed, reversely first accelerate the reciprocal change speed linear motion of periodical high-frequency rate to slow down afterwards, the frequency of reciprocating motion general again
For 5 ~ 1000 times/second, preferably 10-600 times/second.
6. according to the method for claim 1, it is characterised in that：Step（3）The fill factor of the horizontal blending tank is
0.6 ~ 0.8, wherein the fill factor be in blending tank liquid volume with mix the ratio between tank volume.
7. according to the method for claim 1, it is characterised in that：The mixing reactor, including horizontal blending tank, charging
Hose, discharge tube and reciprocator；Inlet port and outlet port are respectively set in the both ends of horizontal blending tank, feed hose
One end connects horizontal blending tank feed inlet, other end connection charging, and one end of discharge tube connects the discharge port of horizontal blending tank,
Other end connection discharging；Reciprocator include two parallel guide rails, spring, sliding block or wheel, pedestal II, fixed seat,
Driving device and sliding rack；Wherein sliding rack includes pedestal I and connecting plate；Two parallel guide rails are horizontal positioned, fixed seat pair
Claim the inside for being fixed on two guide rail left and right ends, is connected by spring between fixed seat and pedestal II；Sliding rack and 4 fixations
Seat be in same plane, for the vertical guide rail direction of the left and right sides 2 pedestal I and be parallel to guide rail two connecting plates constitute
Rectangular configuration；Wherein pedestal I is strip, and length is slightly less than the spacing of two closed slides, below connecting plate installation sliding block or
Wheel, sliding block or wheel are equipped with groove, and rail crown is equipped with longitudinal ridge, longitudinal ridge and sliding block or the wheel of guide rail along its length
Groove occlusion；Horizontal blending tank is fixed on the sliding rack of reciprocator；Driving device and pedestal I or pedestal II phases
Even.
8. according to the method for claim 7, it is characterised in that：Sliding block or wheel are arranged symmetrically, and number is at least 2 pairs.
9. according to the method for claim 7, it is characterised in that：In mixing reactor between the longitudinal ridge of two closed slides
Away from 1.1-1.5 times for blending tank diameter.
10. according to the method for claim 7, it is characterised in that：Two pieces of connecting plates of horizontal blending tank and sliding rack are fixed
Connection.
11. according to the method for claim 7, it is characterised in that：Ranging from sliding between the fixed seat of guide rail left and right ends
The reciprocating motion space of frame；Horizontal blending tank on sliding rack does reciprocating linear fortune along guide rail between the fixed seat of left and right ends
Dynamic, pedestal I is periodically collided and is contacted in reciprocatory movement with pedestal II.
12. according to the method for claim 7, it is characterised in that：Driving device uses electronic, pneumatic, hydraulic-driven or magnetic
One kind in power drive.
13. a kind of system producing biodiesel, includes mainly：Premixing tank, air and liquid mixer, mixing reactor, ejector and
Products pot；Grease feed inlet, alcohols feed inlet and premix material outlet is arranged in premixing tank；Air and liquid mixer be equipped with fluid inlet,
Gas phase import and the outlet of gas-liquid mixed material；Mixing reactor includes horizontal blending tank, feed hose, discharge tube and reciprocal fortune
Dynamic device；Material inlet, refluxing opening, outlet for product and gas vent is arranged in products pot；The premix material outlet of premixing tank passes through
The fluid inlet of pipeline and air and liquid mixer connects, the charging of gas-liquid mixed the material outlet and mixing reactor of air and liquid mixer
Hose connects, and the discharge tube of mixing reactor connect with ejector feed entrance, ejector export through pipeline and products pot into
Mouthful connection, product pot bottom are equipped with phegma and export, and phegma is exported and connect with ejector reflux inlet through pipeline, and gas is from production
After the gas vent outflow of product tank, returns again to gas phase import and recycle.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710066669.4A CN108395937B (en) | 2017-02-07 | 2017-02-07 | Method and system for producing biodiesel |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710066669.4A CN108395937B (en) | 2017-02-07 | 2017-02-07 | Method and system for producing biodiesel |
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| Publication Number | Publication Date |
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| CN108395937A true CN108395937A (en) | 2018-08-14 |
| CN108395937B CN108395937B (en) | 2021-05-04 |
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|---|---|---|---|
| CN201710066669.4A Active CN108395937B (en) | 2017-02-07 | 2017-02-07 | Method and system for producing biodiesel |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114682208A (en) * | 2022-04-23 | 2022-07-01 | 宁波杰森绿色能源科技有限公司 | Continuous desulfurization and deacidification system and method |
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|---|---|---|---|---|
| CN101717696A (en) * | 2009-11-03 | 2010-06-02 | 朱瑞林 | Technological method and equipment for preparing biodiesel by using palm oil |
| CN104024211A (en) * | 2011-08-26 | 2014-09-03 | 浦项产业科学研究院 | Method for producing biodiesel |
| CN205216720U (en) * | 2015-12-04 | 2016-05-11 | 广东和平君乐药业有限公司 | Two -dimensional motion mixer |
-
2017
- 2017-02-07 CN CN201710066669.4A patent/CN108395937B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101717696A (en) * | 2009-11-03 | 2010-06-02 | 朱瑞林 | Technological method and equipment for preparing biodiesel by using palm oil |
| CN104024211A (en) * | 2011-08-26 | 2014-09-03 | 浦项产业科学研究院 | Method for producing biodiesel |
| CN205216720U (en) * | 2015-12-04 | 2016-05-11 | 广东和平君乐药业有限公司 | Two -dimensional motion mixer |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114682208A (en) * | 2022-04-23 | 2022-07-01 | 宁波杰森绿色能源科技有限公司 | Continuous desulfurization and deacidification system and method |
| CN114682208B (en) * | 2022-04-23 | 2024-01-26 | 宁波杰森绿色能源科技有限公司 | Continuous desulfurization and deacidification system and method |
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| Publication number | Publication date |
|---|---|
| CN108395937B (en) | 2021-05-04 |
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