CN205258426U - Preparation biodiesel's ester exchange tower cauldron formula consecutive reaction device - Google Patents
Preparation biodiesel's ester exchange tower cauldron formula consecutive reaction device Download PDFInfo
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- CN205258426U CN205258426U CN201521114123.4U CN201521114123U CN205258426U CN 205258426 U CN205258426 U CN 205258426U CN 201521114123 U CN201521114123 U CN 201521114123U CN 205258426 U CN205258426 U CN 205258426U
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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
- 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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Abstract
The utility model discloses a preparation biodiesel's ester exchange tower cauldron formula consecutive reaction device, including reation kettle, be provided with inlet pipe and discharging pipe on it, the device also has raw materials conveying system and water conservancy diversion control system: raw materials conveying system includes raw materials filling pipe, delivery pump and heater, raw materials filling pipe on be provided with a plurality of raw materials filler, this raw materials filling pipe with delivery pump intercommunication, the delivery pump passes through the feed line intercommunication with the inlet pipe, the heater sets up on feed line, and this heater is multitube pipeline reactor for for the raw materials heating and with the material misce bene, in order to increase reaction rate. Water conservancy diversion control system includes frequency modulation motor and three leaf helical agitator, frequency modulation motor adjustment at reation kettle's top, through the connecting rod with be located reation kettle three leaf helical agitator fixed connection. The utility model has the advantages of continuous production, difficult block up, the product conversion rate is high, output is high.
Description
Technical field
The utility model belongs to chemical industry equipment field, relates in particular to the consersion unit of biodiesel, is specifically related to a kind of systemThe transesterification column autoclave continuous reaction apparatus of standby biodiesel.
Background technology
Biodiesel is originated as primary raw material mainly with vegetable oil and animal tallow, and domestic industry is produced biological bavin at presentOil mainly contains two kinds of methods, one be by low swill wet goods acid value oil after refining, directly adopt ester-interchange method to reactBiodiesel processed; Another kind is to adopt the high grease of acid value first to carry out esterification, and most of aliphatic acid is converted into aliphatic acidEster, after acid value reduces, then carries out ester exchange reaction. No matter which kind of method all needs to carry out ester exchange reaction.
The ester exchange reaction of biodiesel normally utilizes reactor to carry out, and raw material is placed in to still, treats that this batch of raw material disappearsAfter consumption, product is derived, then add new raw material to react. Ester-exchange reaction is interrupted like this, Bu NenglianContinuous production, thereby every batch of raw material all will carry out preheating, add the operations such as catalyst, energy consumption is high, complicated operation, production cycle are long. MirrorIn this, once there is part producing enterprise to attempt adopting the pipe reaction device of continous way to carry out alternative reaction still, but because China is rawThing diesel raw material mostly is waste grease, wherein contains a certain amount of impurity, therefore often occurs line clogging phenomenon.
Because ester exchange reaction is reversible reaction, obviously will react afterproduct and discharge (being mainly glycerine), be more conducive to turnThe raising of rate. But at present conventional biodiesel production method be still the method that strengthens reaction raw materials dosage make chemical balance toThe direction that increases reaction afterproduct tilts---and excessive alcohol (being mainly methyl alcohol) is added in ester interchange vessel and participates in reaction, conventionallyAlcohol and the mol ratio of grease be 6:1(be about react 2 times of aequum), and then excessive alcohol is removed. This production technologyThere is open defect: the one, the use amount of methyl alcohol is large, and well-known methyl alcohol is inflammable and explosive and have toxicity, and a large amount of use has safetyRisk; The 2nd, the amount that increases reaction afterproduct by increasing the method for raw material has been improved the standard to the productive rate of reaction afterproductLimit.
Therefore, how to make the production equipment that carries out ester exchange reaction realize nonclogging quantity-produced simultaneously, can show againWork improves the conversion ratio of product, is a unsolved difficult problem still in industrial biological diesel production.
Summary of the invention
For prior art above shortcomings, the purpose of this utility model is to provide one can realize continuous lifeProduce, be difficult for stopping up, the transesterification column autoclave continuous reaction apparatus of preparation biodiesel that conversion rate of products is high.
To achieve these goals, the technical solution adopted in the utility model is as follows:
A transesterification column autoclave continuous reaction apparatus of preparing biodiesel, comprises reactor, and this reactor is provided withFeed pipe and discharge nozzle, is characterized in that, also comprises source material delivery system and flow controlling system; Described source material delivery systemComprise raw material filler pipe, delivery pump and heater; On described raw material filler pipe, be provided with several for annotating raw material or urgeThe raw material filler of agent, this raw material filler pipe is communicated with described delivery pump, and described delivery pump and feed pipe pass through raw materialCarrier pipe is communicated with; Described heater is arranged on feed line, and this heater is multitubular reactor; Described flow controllingSystem comprises frequency modulation motor and three leaf spiral agitators; Described frequency modulation motor is adjusted at the top of reactor, by connecting rod withThe described three leaf spiral agitators that are positioned at reactor are fixedly connected with.
Further, described flow controlling system also comprises and is positioned at reactor and the guide shell parallel with its inwall, shouldGuide shell is fixed on the centre of described reactor, and upper and lower end is uncovered and does not contact with described reactor; Three described leavesSpiral agitator is positioned at the top of described guide shell, and the port of export of described feed pipe is positioned at described guide shell, and inThe below of three described leaf spiral agitators.
Further, the entrance point of described discharge nozzle and the port of export of described feed pipe are on same horizontal line.
Further, on described frequency modulation motor, arrange with decelerator, for adjusting the rotating speed of described three leaf spiral agitators.
Further, the inside of described reactor and feed pipe is respectively arranged with temperature sensor.
Further, on described raw material filler pipe, feed line, discharge nozzle and raw material filler, be provided with valve.
Further, the lower end of described reactor is provided with return duct, and this return duct is communicated with described raw material filler pipe;On described return duct, be provided with flow-stop valve, for controlling the capacity of returns of the material in described reactor.
Further, on described discharge nozzle, be provided with sample tap, for inspection by sampling.
Further, the rotating speed of three described leaf spiral agitators is 80-400rpm.
Further, the ratio of height to diameter of described reactor is 3 ~ 4:1.
Compared with prior art, the utlity model has following beneficial effect:
1, the utility model is that tower reactor formula reaction vessel designs in conjunction with adjustable pipe reaction, and ester exchange reaction is removed at towerIn still reaction container, continous-stable carries out, outside can not stopping up; In the pipeline of simultaneously carrying at pump and heater, all carry out continuouslyReaction, can not stop gathering because the circulation of pump makes material, has reduced obstruction, simultaneously due to non-former in the middle of the part in materialMaterial material active matter exists, and makes the reduced viscosity of material, and intermiscibility is better, does not only have the blockage problem of pipeline reactor,Also strengthen reaction process.
2, derive because the utility model will react afterproduct, impel ester exchange reaction to being conducive to reaction of formation afterproductDirection carry out, thereby improved widely the conversion ratio of product.
3, because the utility model is by the direction of the direction control chemical reaction of reaction afterproduct derivation, thereby greatly subtractLack alcohols, the especially use amount of methyl alcohol, security improves greatly.
4,, owing to being successive reaction, the viscosity by product on whole system, the impact of intermiscibility, make reaction speedAccelerate, and reduced the consumption of catalyst
5, the utility model does not need to carry out every still charging, discharging operation, and the operating personnel that need are few, and cost is low.
6, compared with the discontinuous reactor of the utility model and same volume, output is significantly increased.
Brief description of the drawings
Fig. 1 is structural representation of the present utility model;
In accompanying drawing: 1-reactor; 10-guide shell; 11-feed pipe; 12-discharge nozzle; 121-sample tap; 21-formerMaterial filler pipe; 211-raw material filler; 22-delivery pump; 23-feed line; 24-heater; 31-three leaf spirals stirMix device; 32-frequency modulation motor; 33-decelerator; 4-temperature sensor; 5-return duct; 51-flow-stop valve.
Detailed description of the invention
Below in conjunction with specific embodiment, the utility model is described in further detail.
One, a transesterification column autoclave continuous reaction apparatus of preparing biodiesel, as shown in Figure 1, comprises reactor 1,This reactor 1 is provided with feed pipe 11 and discharge nozzle 12, it is characterized in that, also comprises source material delivery system and flow controlling systemSystem; Described source material delivery system comprises raw material filler pipe 21, delivery pump 22 and heater 24; On described raw material filler pipe 21Be provided with several and use raw material filler 211, the materials such as feedstock oil, methyl alcohol and catalyst of can annotating respectively; This raw material fillingPipe 21 is communicated with described delivery pump 22, and described delivery pump 22 is communicated with by feed line 23 with feed pipe 11; DescribedHeater 24 is arranged on feed line 23, and this heater 24 is multitubular reactor, for giving heating raw materials, simultaneously because of its toolThere is the function of multitubular reactor, can promote raw material to mix, and in multitube, carry out ester exchange reaction, improve reaction rate; ItsReason is, heater 24 can be in meeting heating material circulation, and the conveying that utilizes the outlet of delivery pump 22 to exist is pressedPower, makes ester exchange reaction speed faster.
Described flow controlling system comprises frequency modulation motor 32 and three leaf spiral agitators 31; Described frequency modulation motor 32 is adjustedWhole at the top of reactor 1, be fixedly connected with the described three leaf spiral agitators 31 that are positioned at reactor 1 by connecting rod.
As one preferred embodiment, described flow controlling system also comprise be positioned at reactor 1 and with itsThe guide shell 10 that wall is parallel, this guide shell 10 is fixed on the centre of described reactor 1, and it is uncovered and not with described that upper and lower end isReactor 1 contact; Three described leaf spiral agitators 31 are positioned at the top of described guide shell 10, the going out of described feed pipe 11Mouthful end is positioned at described guide shell 10, and below in three described leaf spiral agitators 31. The use of guide shell 10 canSo that material flows downward therein, Flow of Goods and Materials is behind reactor 1 bottom, in the turning effort of three leaf spiral agitators 31Lower spatial flow between guide shell 10 and reactor 1 inwall, then under the impetus of the new raw material flowing downward, toUpper flowing, thus the abundant contact that realizes material is to promote reaction to carry out.
As one preferred embodiment, the entrance point of described discharge nozzle 12 and the port of export place of described feed pipe 11On same horizontal line. Be conducive to like this circulation of material.
As one preferred embodiment, on described frequency modulation motor 32, arrange with decelerator 33, described in adjustingThe rotating speed of three leaf spiral agitators 31, to adapt to the reaction requirement of different material.
As one preferred embodiment, the inside of described reactor 1 and feed pipe 11 is respectively arranged with temperature biographySensor 4, is convenient to monitor reaction temperature.
As one preferred embodiment, described raw material filler pipe 21, feed line 23, discharge nozzle 12 and raw materialOn filler 211, be provided with valve, to adjust flow velocity, the flow of material.
As one preferred embodiment, the lower end of described reactor 1 is provided with return duct 5, this return duct 5 and instituteThe raw material filler pipe 21 of stating is communicated with; On described return duct 5, be provided with flow-stop valve 51, for controlling the thing in described reactor 1The capacity of returns of matter.
As one preferred embodiment, on described discharge nozzle 12, be provided with sample tap 121, for inspection by sampling.
As one preferred embodiment, the rotating speed of three described leaf spiral agitators 31 is 80-400rpm.
As one preferred embodiment, the ratio of height to diameter of described reactor 1 is 3 ~ 4:1, to guarantee that material is from enteringStart, finish discharging to reaction, product meets designing requirement.
Operation as follows in actual production:
As Fig. 1, feedstock oil, methyl alcohol, catalyst are carried to heater via 24 by raw material by delivery pump 22, be heated to 65 DEG CAfter～67 DEG C, enter the below of three leaf spiral agitators 31 in the guide shell 10 of reactor 1; Three leaf spiral agitators 31 with leadStream cylinder 10 by the material of coming in along the interior downward conveying of guide shell 10. While operation first, flow-stop valve 51 should be closed, and makes material from leadingStream cylinder 10 is interior through the reactor 1 backward guide shell 10 space outerpace circulations in bottom. When initial charge, discharge nozzle 12 is in cutting out shapeState, material circulates always in still, waits material in still to be all full of rear maintenance recurrent state, closes all raw material fillers simultaneouslyThe valve at 211 places, and sample and check its glycerin ratio at sample tap 121 use sampling graduated cylinders, when lower floor's material in sampling graduated cylinderWhen (glycerine and methyl alcohol) reaches approximately 9%, open the valve at raw material filler 211 places, make feedstock oil, methyl alcohol, catalyst by fixing ratioExample and flow charging; Open discharging opening simultaneously, make the flow of input and output material identical.
According to need of production, can open flow-stop valve 51, make the partial material in reactor 1 enter raw material through return duct 5Filler pipe 21 is re-circulated in reactor 1, to promote material movement and to keep reaction temperature.
The stirring motor of this device is frequency modulation motor 32, by reductor, the rotating speed of three leaf spiral agitators 31 is controlled atBetween 80-400 turns; The three leaf spiral agitators 31 of this device make mixed material in still all be spiral in guide shell 10 and outside cylinderShape, once normal continuous discharge, it is constant that its rotating speed must keep.
This device can be used in conjunction with other devices, and reaction afterproduct is discharged from discharge nozzle 12, and upper materials (is mainlyCrude fatty acid methyl ester) separate with lower floor's material (glycerine and methyl alcohol); Lower floor's material is imported to glycerine and equipment for separating methanol, by sweetOil and separating methanol. Import the device identical with Fig. 1 using upper materials as feedstock oil, supplement a small amount of methyl alcohol and catalyst and enterRow reaction. Originally the material that installs out from the second cover separates again, and lower floor's material enters another glycerine and separating methanol againDevice, upper materials enters precipitation, distillation operation can obtain refined biometric diesel oil.
This device reaction process remains high reynolds number Re, and temperature constant within the specific limits, there will not be obstruction;Continuous operation after driving, conversion rate of products is high. Due to all airtight carrying out of whole process, the gas phase of having avoided discontinuous device to bringThe impact that volatilization brings to environment.
Two, embodiment
For the raw material of different qualities, the flow parameter of the material in reactor 1 can be controlled, thereby make reactionMaterial be blended in optimum state; The utility model control reaction mass temperature, between 65 DEG C～67 DEG C, makes it a little more than first64.7 DEG C of the boiling points of alcohol, granularity that methyl alcohol is distributed is thinner, specific surface area is larger, and this is conducive to accelerate reaction rate, shorteningReaction time. Utilize the utility model to carry out contrast test to the reaction of different acid value materials, its result is as follows in table 1:
The raw material contrast test of the different acid values of table 1
| Project | Test 1 | Test 2 | Test 3 | Test 4 |
| Feedstock oil acid value | 0.5 | 1.0 | 1.5 | 2 |
| Methanol consumption (%) | 11.4 | 11.4 | 11.4 | 11.4 |
| NaOH consumes (%) | 0.54 | 0.58 | 0.63 | 0.68 |
| Conversion rate of products (%) | 98.5 | 97.5 | 96 | 95 |
In table 1, methanol consumption, NaOH consumption are all taking the weight of feedstock oil as 100% calculating; Wherein, NaOH isThe high feedstock oil of acid value adds and produces owing to first reacting with it to make after sodium methoxide with methyl alcohol, because need be added a certain amount of alkaliNeutralization, carrying out smoothly of guarantee reaction, also can reduce the corrosion of acidic materials to chemical industry equipment simultaneously.
As can be seen from Table 1, though acid value up to 2 o'clock, its conversion ratio has also reached 95%, and the utility model is in acid valueNot higher than 1.5 o'clock, lowermost turn rate also can reach 96%, and this index is far above the conversion ratio of discontinuous reactor.
As to adopt two cover volumes be 20m3The utility model (successively connect), after first set, increase sedimentation continuous separate fromDevice, logical isolation of intermediate products glycerine; Then react not only output and can reach 300T/ days continuing to enter the second cover, far aboveThe output that two discontinuous reactors are 180 tons/day; In energy consumption, react far below being interrupted simultaneously; On conversion ratio at least thanDisconnected reaction is high by 4%.
Above-described embodiment of the present utility model is to be only explanation the utility model example, and is not to this realityWith the restriction of novel embodiment. For those of ordinary skill in the field, also can on the basis of the above descriptionTo make other multi-form variation and variations. Here cannot give exhaustive to all embodiments. Every this reality that belongs toThe apparent variation of amplifying out by novel technical scheme or the still row in protection domain of the present utility model of variation.
Claims (10)
1. a transesterification column autoclave continuous reaction apparatus of preparing biodiesel, comprises reactor, this reactor be provided with intoMaterial pipe and discharge nozzle, is characterized in that, also comprises source material delivery system and flow controlling system;
Described source material delivery system comprises raw material filler pipe, delivery pump and heater; On described raw material filler pipe, be provided withSeveral are for the raw material filler of annotate raw material or catalyst, and this raw material filler pipe is communicated with described delivery pump, describedDelivery pump is communicated with by feed line with feed pipe; Described heater is arranged on feed line, and this heater is manyPipe reactor;
Described flow controlling system comprises frequency modulation motor and three leaf spiral agitators; Described frequency modulation motor is adjusted at reactorTop, be fixedly connected with the described three leaf spiral agitators that are positioned at reactor by connecting rod.
2. the transesterification column autoclave continuous reaction apparatus of preparation biodiesel according to claim 1, is characterized in that instituteThe flow controlling system of stating also comprises and is positioned at reactor and the guide shell parallel with its inwall, and this guide shell is fixed on described anti-Answer the centre of still, upper and lower end is uncovered and does not contact with described reactor; Described in three described leaf spiral agitators are positioned atThe top of guide shell, the port of export of described feed pipe is positioned at described guide shell, and stirs in three described leaf spiralsThe below of device.
3. the transesterification column autoclave continuous reaction apparatus of preparation biodiesel according to claim 2, is characterized in that instituteThe entrance point of the discharge nozzle of stating and the port of export of described feed pipe are on same horizontal line.
4. the transesterification column autoclave continuous reaction apparatus of preparation biodiesel according to claim 1, is characterized in that instituteOn the frequency modulation motor of stating, arrange with decelerator, for adjusting the rotating speed of described three leaf spiral agitators.
5. the transesterification column autoclave continuous reaction apparatus of preparation biodiesel according to claim 1, is characterized in that instituteThe reactor of stating and the inside of feed pipe are respectively arranged with temperature sensor.
6. the transesterification column autoclave continuous reaction apparatus of preparation biodiesel according to claim 1, is characterized in that instituteOn raw material filler pipe, feed line, discharge nozzle and the raw material filler of stating, be provided with valve.
7. according to the transesterification column autoclave continuous reaction apparatus of the arbitrary described preparation biodiesel of claim 1-6, its featureBe, the lower end of described reactor is provided with return duct, and this return duct is communicated with described raw material filler pipe; Described backflowOn pipe, be provided with flow-stop valve, for controlling the capacity of returns of the material in described reactor.
8. the transesterification column autoclave continuous reaction apparatus of preparation biodiesel according to claim 7, is characterized in that instituteOn the discharge nozzle of stating, be provided with sample tap, for inspection by sampling.
9. the transesterification column autoclave continuous reaction apparatus of preparation biodiesel according to claim 4, is characterized in that instituteThe rotating speed of the three leaf spiral agitators of stating is 80-400rpm.
10. the transesterification column autoclave continuous reaction apparatus of preparation biodiesel according to claim 1, is characterized in that,The ratio of height to diameter of described reactor is 3 ~ 4:1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201521114123.4U CN205258426U (en) | 2015-12-29 | 2015-12-29 | Preparation biodiesel's ester exchange tower cauldron formula consecutive reaction device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201521114123.4U CN205258426U (en) | 2015-12-29 | 2015-12-29 | Preparation biodiesel's ester exchange tower cauldron formula consecutive reaction device |
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| CN205258426U true CN205258426U (en) | 2016-05-25 |
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| CN201521114123.4U Expired - Fee Related CN205258426U (en) | 2015-12-29 | 2015-12-29 | Preparation biodiesel's ester exchange tower cauldron formula consecutive reaction device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107287037A (en) * | 2017-07-27 | 2017-10-24 | 湖南华远新能源有限公司 | A kind of biodiesel esterification device and technique |
| CN110878232A (en) * | 2019-12-01 | 2020-03-13 | 江西艾迪尔新能源有限公司 | Device for preparing biodiesel through rapid reaction of rotary fixed bed |
-
2015
- 2015-12-29 CN CN201521114123.4U patent/CN205258426U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107287037A (en) * | 2017-07-27 | 2017-10-24 | 湖南华远新能源有限公司 | A kind of biodiesel esterification device and technique |
| CN110878232A (en) * | 2019-12-01 | 2020-03-13 | 江西艾迪尔新能源有限公司 | Device for preparing biodiesel through rapid reaction of rotary fixed bed |
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20160525 Termination date: 20201229 |