CN203474763U - Continuous ester exchange reactor and device - Google Patents
Continuous ester exchange reactor and device Download PDFInfo
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- CN203474763U CN203474763U CN201320457888.2U CN201320457888U CN203474763U CN 203474763 U CN203474763 U CN 203474763U CN 201320457888 U CN201320457888 U CN 201320457888U CN 203474763 U CN203474763 U CN 203474763U
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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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- 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
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/30—Wastewater or sewage treatment systems using renewable energies
- Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy
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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
The utility model discloses a continuous ester exchange reactor and a continuous ester exchange reaction device. The continuous ester exchange reactor comprises an ester exchange reaction kettle and a stirring device; a mixed material inlet is formed in the bottom of the ester exchange reaction kettle; a mixed material outlet is formed in the upper part of the ester exchange reaction kettle; a plurality of partition plates are arranged in the ester exchange reaction kettle and used for dividing an inner cavity of the ester exchange reaction kettle into a plurality of cavities; a steam adjoining tube is arranged on the inner wall of the ester exchange reaction kettle; a steam inlet and a steam outlet are respectively formed in the two ends of the steam adjoining tube; the stirring device comprises a stirring motor, a stirring shaft and stirring blades, wherein the stirring shaft and the stirring motor are connected and are arranged in the ester exchange reaction kettle from top to bottom, and the stirring blades are arranged on the stirring shaft. The continuous ester exchange reaction device is the continuous ester exchange reaction device comprising the continuous ester exchange reactor. The continuous ester exchange reaction device disclosed by the utility model can be utilized to carry out a continuous ester exchange reaction, and can be used for large-scale continuous industrial production.
Description
Technical field
The utility model belongs to biofuel Preparation equipment technical field, particularly a kind of continuous ester interchange reactor and device.
Background technology
In the raw material of existing production biofuel, high-acid value grease, if hogwash fat, sewer oil and acidifying wet goods are exactly the raw material of very suitable preparation biofuel.Utilize high-acid value grease can solve the problem that returns to dining table of food and beverage waste oil and grease on the one hand as the raw material of production biofuel, reduced on the other hand the production cost of biofuel, therefore, utilize producing biodiesel from high acid number grease to there is good Social benefit and economic benefit.
In the prior art, utilize high acid value grease production biofuel all to need to carry out esterification or ester interchange treatment, the equipment that carries out at present esterification treatment is a lot, and English Patent GB143069 discloses a kind of tank reactor, and this reactor erosion resistance is not high and can not be to react continuously to carry out; German patent DE 19610564 discloses and has a kind ofly adopted a plurality of tank reactor series systems for the method for biofuel, and it adopts rhythmic reaction to be unfavorable for that the continuous industry of mass-producing produces; Japanese Patent JP3115249 discloses a kind of reactor in elevated pressures (0.25～2.5MPa) and the lower preparation of comparatively high temps (150～350 ℃) biofuel, and this equipment requirements is high, complicated operation; World patent WO9008127 discloses a kind of bed tubular reactor, under certain pressure, just can react.Aforesaid device all exists that preparation cost is high, shortcoming that can not successive reaction, and the continuous industry that is difficult to use in mass-producing is produced.
Utility model content
The purpose of this utility model is to overcome the deficiencies in the prior art, and a kind of continuous ester interchange reactor is provided, and utilizes this continuous ester interchange reactor can carry out continuous transesterification reaction.The applicant's application number be 201210447693.X, name be called " alkali refining byproduct-soap stock recycle and technique of zero discharge in vegetable oil refining " in first to file, the preliminary technical scheme that has provided this continuous ester interchange reactor, the utility model will be described in further detail it.
Another object of the present utility model is to provide a kind of continuous esterification device that comprises above-mentioned continuous ester interchange reactor.
The technical scheme that the utility model is realized above-mentioned purpose is:
A continuous ester interchange reactor, comprises transesterification reactor and whipping appts, and wherein, the bottom of transesterification reactor is provided with compound import, and top is provided with compound outlet; In transesterification reactor, be provided with polylith dividing plate the inner chamber of transesterification reactor is separated into a plurality of cavitys; The inwall of transesterification reactor is provided with steam adjoining pipe, and the two ends of this steam adjoining pipe are respectively equipped with steam inlet and vapour outlet; Described whipping appts comprises agitator motor, stir shaft and paddle, and wherein, stir shaft is connected with agitator motor, and is arranged on from top to bottom in transesterification reactor, and described paddle is located on stir shaft.
Described dividing plate is three, is vertically equidistantly arranged in transesterification reactor, from top to bottom the inner chamber of transesterification reactor is divided into A, B, C, tetra-cavitys of D; Described agitator motor is arranged on the central authorities at the top of transesterification reactor; The upper end of described stir shaft is connected with agitator motor, and lower end is connected with the bearing that is located at transesterification reactor bottom, and whole stir shaft passes described dividing plate, and between stir shaft and dividing plate, has the gap of the Flow of Goods and Materials of allowing, and a paddle is set in each cavity.
Described compound import is arranged on the bottom centre of D cavity; Described compound outlet is arranged at the upper right corner of A cavity; Described steam inlet is arranged at the upper left corner of A cavity; Described vapour outlet is arranged at the lower right corner of D cavity.
Described steam adjoining pipe is spirally coiled on transesterification reactor inwall.
A continuous ester interchange reaction unit that comprises above-mentioned continuous ester interchange reactor, also comprises stock oil drawing-in device, auxiliary material drawing-in device and material discharger, wherein:
Described stock oil drawing-in device comprises the temporary tank of the stock oil connecting successively, stock oil feeding pump, interchanger and stock oil flow director;
Described auxiliary material drawing-in device comprises the auxiliary material connecting successively temporary tank, auxiliary material feeding pump and auxiliary material flow director;
Described stock oil drawing-in device and auxiliary material drawing-in device are connected in parallel on mixing tank, and this mixing tank is connected with the compound import of transesterification reactor by pipeline;
Described material discharger comprises the standing separation device in the compound outlet that is connected to transesterification reactor.
Described material discharger also comprises that light phase materials is kept in tank, gently phase materials discharging pump, heavy phase material are kept in tank and heavy phase material discharging pump, wherein, the temporary tank of described light phase materials and light phase materials discharging pump are serially connected in the top of standing separation device, and the temporary tank of described heavy phase material and heavy phase material discharging pump are serially connected in the bottom of standing separation device.
On described mixing tank, be also connected in parallel to standby temporary tank and standby feeding volume pump.
On described interchanger and transesterification reactor, be connected to respectively temperature regulator A and temperature regulator B.
Described transesterification reactor is provided with tensimeter, and this tensimeter is arranged at the top of transesterification reactor.
On pipeline between described compound outlet and standing separation device, be also provided with thief hole.
The principle of work of continuous ester interchange reactor of the present utility model is:
The stock and adjunct responding all enters in still from transesterification reactor bottom, hybrid reaction through stirring and progressively, liquid level progressively raises, pass through successively a plurality of cavitys in transesterification reactor, in each cavity, be provided with paddle, all paddles are stir shaft altogether, and material fully reacts through a plurality of cavitys successively in transesterification reactor uphill process, when liquid level is to still top, reaction solution starts to overflow from compound outlet; Due to the continuous charging reaction from bottom, in still, stop and reach the reaction times, from top, continuous overflow discharging, realizes successive reaction, reaches quantity-produced object.
The principle of work of continuous ester interchange reaction unit of the present utility model is:
Material is operated according to preparing biological diesel fuel by high-acid-value grease device systems, start stock oil feeding pump, auxiliary material feeding pump (standby feeding volume pump) simultaneously, regulate stock oil flow director and auxiliary material flow director (standby feeding volume pump) to set raw material, auxiliary material (standby material) flow per hour simultaneously, reach material reaction optimum proportion; Open interchanger steam valve, regulate temperature regulator B to set temperature of reaction; When being full of mixing tank, liquid phase material starts mixing tank; Raw material, auxiliary material (standby material) with proper ratio, according to the speed of setting, enter transesterification reactor and react, liquid level progressively rises; Reach the reaction times of design, at the reaction mass of continuous ester interchange reactor, be completely full of while reaching compound outlet, it is separated that the overflow of material nature enters standing separation device, isolates upper strata and be light phase materials, the lower floor phase materials of attaching most importance to.
The utility model compared with prior art has following beneficial effect:
1, in continuous ester interchange reactor of the present utility model, material enters from the bottom of transesterification reactor, material fully mixes and reacts by stirring in transesterification reactor uphill process, according to the calculating residence time in reaction times, according to residence Time Calculation volume, thereby assurance successive reaction, reaches quantity-produced object.Described dividing plate can adopt detachable structure, has both guaranteed the reaction times, has prevented short circuit, is convenient to again cleaning, maintenance.
2, in continuous ester interchange reactor of the present utility model, adopt steam adjoining pipe to mix heat, improved thermal conversion efficiency, strengthened again the casing rigidity of equipment.
3, continuous ester interchange structure of reactor of the present utility model is simple, takes up room little, with low cost, can carry out successive reaction, can produce for the continuous industry of mass-producing.
4, continuous ester interchange reaction unit of the present utility model, in conjunction with the advantage of continuous ester interchange reactor, for continuous esterification provides complete equipment.
Accompanying drawing explanation
Fig. 1 is the structural representation of an embodiment of continuous ester interchange reactor of the present utility model.
Fig. 2 is the workflow schematic diagram of continuous ester interchange reactor shown in Fig. 1.
Fig. 3 is the structural representation of an embodiment of continuous ester interchange reaction unit of the present utility model.
In figure, Reference numeral is:
1-stock oil is kept in tank, 2-auxiliary material is kept in tank, the standby temporary tank of 3-, 4-stock oil feeding pump, 5-auxiliary material feeding pump, the standby feeding volume pump of 6-, 7-stock oil flow director, 8-auxiliary material flow director, 9-interchanger, 10-temperature regulator A, 11-mixing tank, 12-temperature regulator B, 13-whipping appts, 14-tensimeter, 15-continuous ester interchange reactor, 16-standing separation device, 17-thief hole, the light phase materials of 18-is kept in tank, the light phase materials discharging pump of 19-, 20-heavy phase material is kept in tank, 21-heavy phase material discharging pump, the import of 22-compound, the outlet of 23-compound, 24-agitator motor, 25-stir shaft, 26-paddle, 27-dividing plate, 28-steam inlet, 29-vapour outlet, 30-steam adjoining pipe, 31-transesterification reactor.
Embodiment
Below in conjunction with embodiment and accompanying drawing, the utility model is described in further detail, but embodiment of the present utility model is not limited to this.
Embodiment 1
Referring to Fig. 1 and Fig. 3, the continuous ester interchange reactor 15 of the present embodiment, comprises transesterification reactor 31 and whipping appts 13.Wherein, the bottom of transesterification reactor 31 is provided with compound import 22, and top is provided with compound outlet 23.In transesterification reactor 31, be provided with three dividing plates 27, be vertically equidistantly arranged on the inwall of transesterification reactor 31, from top to bottom the inner chamber of transesterification reactor 31 is divided into A, B, C, tetra-cavitys of D.On the inwall of transesterification reactor 31, helical disk is wound with steam adjoining pipe 30, and the two ends of this steam adjoining pipe 30 are respectively equipped with steam inlet 28 and vapour outlet 29.Described whipping appts 13 comprises agitator motor 24, stir shaft 25 and paddle 26, and wherein, described agitator motor 24 is arranged on the central authorities at the top of transesterification reactor 31; The upper end of described stir shaft 25 is connected with agitator motor 24, lower end is connected with the bearing that is located at transesterification reactor 31 bottoms, whole stir shaft 25 passes described dividing plate 27, and between stir shaft 25 and dividing plate 27, has the gap of the Flow of Goods and Materials of allowing, and a paddle 26 is set in each cavity.
Referring to Fig. 1, described compound import 22 is arranged on the bottom centre of D cavity; Described compound outlet 23 is arranged at the upper right corner of A cavity, and (in the utility model, described upper and lower, left and right are all to determine with the view shown in Fig. 1.); Described steam inlet 28 is arranged at the upper left corner of A cavity; Described vapour outlet 29 is arranged at the lower right corner of D cavity.
Below in conjunction with accompanying drawing, the principle of work of the continuous esterification device of the present embodiment is further described:
Referring to Fig. 1 and Fig. 2, the stock and adjunct responding all enters in still from transesterification reactor 3110 bottoms, hybrid reaction through stirring and progressively, liquid level progressively raises, pass through successively tetra-cavitys of D, C, B, A of transesterification reactor 31, in each cavity, be provided with paddle 26, all paddles 26 are stir shaft 25 altogether, material fully reacts through 4 internal cavities successively in transesterification reactor 31 uphill process, when liquid level is to still top, reaction solution starts to overflow from compound outlet 23; Due to the continuous charging reaction from bottom, in still, stop and reach the reaction times, from top, continuous overflow discharging, realizes successive reaction, reaches quantity-produced object.
Embodiment 2
The present embodiment provides a kind of continuous ester interchange reaction unit that comprises above-mentioned continuous ester interchange reactor 15, also comprises stock oil drawing-in device, auxiliary material drawing-in device and material discharger.Wherein:
Described stock oil drawing-in device comprises the temporary tank 1 of the stock oil connecting successively, stock oil feeding pump 4, interchanger 9 and stock oil flow director 7, wherein, is connected to temperature regulator A10 on interchanger 9, for controlling the feeding temperature of stock oil.By this stock oil drawing-in device, stock oil is transported in transesterification reactor 31.
Described auxiliary material drawing-in device comprises the auxiliary material connecting successively temporary tank 2, auxiliary material feeding pump 5 and auxiliary material flow director 8.By this auxiliary material drawing-in device, auxiliary material is transported in transesterification reactor 31.
Described stock oil drawing-in device and auxiliary material drawing-in device are connected in parallel on mixing tank 11, and this mixing tank 11 is connected with the compound import 22 of transesterification reactor 31 by pipeline.By this mixing tank 11, stock oil and auxiliary material are fully mixed, and then be transported in transesterification reactor 31, be conducive to improve the effect of reaction.Simultaneously, on this mixing tank 11, be also connected in parallel to standby temporary tank 3 and standby feeding volume pump 6, like this, if need the material in standby temporary tank 3 to carry out hybrid reaction, by starting standby feeding volume pump 6, such as in traditional methanol esterification, need to use stock oil, methyl alcohol and sulfuric acid, standby temporary tank 3 can be for storage sulfuric acid.
Described material discharger comprises the standing separation device 16 in the compound outlet 23 that is connected to transesterification reactor 31, and reacted material overflows and enters in standing separation device 16 from compound outlet 23, and standing upper back is light phase materials, the bottom phase materials of attaching most importance to.For light phase materials and heavy phase feed separation are also stored, on standing separation device 16, be also provided with the temporary tank 18 of light phase materials, light phase materials discharging pump 19, the temporary tank 20 of heavy phase material and heavy phase material discharging pump 21, wherein, the temporary tank 18 of described light phase materials and light phase materials discharging pump 19 are serially connected in the top of standing separation device 16, and the temporary tank 20 of described heavy phase material and heavy phase material discharging pump 21 are serially connected in the bottom of standing separation device 16.
Described transesterification reactor 31 is provided with tensimeter 14 and temperature regulator B12, and wherein tensimeter 14 is arranged at the top of transesterification reactor 31, for detection of the pressure in still; Temperature regulator B12 is arranged at the upper left side of transesterification reactor 31, for controlling the temperature of reaction in still.On pipeline between described compound outlet 23 and standing separation device 16, be also provided with thief hole 17.
Below in conjunction with accompanying drawing, the principle of work of the continuous esterification device of the present embodiment is further described:
Referring to Fig. 3, material is operated according to preparing biological diesel fuel by high-acid-value grease device systems, start stock oil feeding pump 4, auxiliary material feeding pump 5 (standby feeding volume pump 6) simultaneously, regulate stock oil flow director 7 and auxiliary material flow director 8 (standby feeding volume pump 6) to set raw material, auxiliary material (standby material) flow per hour simultaneously, reach material reaction optimum proportion; Open interchanger 9 steam valves, regulate temperature regulator B12 to set temperature of reaction; When being full of mixing tank 11, liquid phase material starts mixing tank 11; Raw material, auxiliary material (standby material) with proper ratio, according to the speed of setting, enter continuous ester interchange reactor 31 and react, liquid level progressively rises; Reach the reaction times of design, at the reaction mass of continuous ester interchange reactor 31, be completely full of and reach compound and export at 23 o'clock, the overflow of material nature enters 16 separation of standing separation device, isolates upper strata and be light phase materials, the lower floor phase materials of attaching most importance to.Lower floor's heavy phase material enters the temporary tank 20 of heavy phase material, starts heavy phase material discharging pump 21 heavy phase material is pumped in next procedure; Light phase materials enters the temporary tank 18 of light phase materials, starts light phase materials discharging pump 19 light phase materials is pumped in next procedure.
Embodiment 3
The present embodiment be embodiment 2 continuous ester interchange reaction unit concrete application for example, particularly, be to utilize this continuous ester interchange reaction unit to realize the example of sewer oil continuous esterification.
The sewer oil that by acid value is first 89 (detecting according to national GB-258) is stored in the temporary tank of raw material; Concentration 99.8% methyl alcohol is stored in the temporary tank of auxiliary material; Concentration is that 98% vitriol oil is stored in standby temporary tank.Chamber is tested repeatedly by experiment, confirms to use sewer oil: methyl alcohol: sulfuric acid volume ratio is to be at 1000: 400: 6 proper ratio, 70 ℃ of esterification reaction temperatures;
Start raw material feeding pump, auxiliary material feeding pump, standby feeding volume pump, regulate stock oil flow director, auxiliary material flow director, standby feeding volume pump setting stock oil, methyl alcohol, sulfuric acid throughput ratio per hour is 1000: 400: 6 simultaneously, open interchanger steam valve, regulating temperature regulator B to set esterification reaction temperature is 70 ℃; When being full of mixing tank, material starts mixing tank; Stock oil, methyl alcohol, sulfuric acid enter flow reactor with proper ratio and carry out esterification, guarantee that logistics stops 2h in flow reactor.
When in flow reactor, material overflows and reaches compound outlet and overflow, material flows out naturally, by thief hole, sample detection, measuring esterised oil acid number is 0.96mgKOH/g (detecting according to national GB-258), material enters liquid phase continous way separator, and the light phase materials in upper strata is that sour methyl alcohol, lower floor's heavy phase material are esterised oil; Lower floor's heavy phase material esterised oil flows to the temporary tank of heavy phase material, starts heavy phase material discharging pump and carries out lower step transesterify operation; Light phase materials acid methyl alcohol flows to the temporary tank of light phase materials, starts light phase materials discharging pump and carries out lower step neutralizing acid, separating methanol operation.
Embodiment 4
The present embodiment be embodiment 2 continuous ester interchange reaction unit concrete application for example, particularly, be to utilize this continuous ester interchange reaction unit to realize the example of esterised oil continuous esterification.
First the esterised oil that needs ester interchange treatment is stored in to the temporary tank of raw material; Alkali-methyl alcohol (alkali concn 2.5%) is stored in the temporary tank of auxiliary material.Chamber is tested repeatedly by experiment, confirms to use sewer oil: alkali-methyl alcohol volume ratio is to be at 1000: 530 proper ratio, 50 ℃ of transesterification reaction temperature;
Ejector priming raw material feeding pump, auxiliary material feeding pump, regulate stock oil flow director, auxiliary material flow director setting esterised oil, alkali-methyl alcohol throughput ratio per hour is 1000: 530 simultaneously; Open interchanger steam valve, regulating temperature regulator B to set esterification reaction temperature is 50 ℃; When being full of mixing tank, material starts mixing tank; Stock oil, alkali-methyl alcohol enter flow reactor with proper ratio and carry out transesterification reaction, guarantee that logistics stops 1h in flow reactor.
When in flow reactor, material overflows and reaches compound outlet and overflow, material flows out naturally, by thief hole, samples detection, and detection transesterify is complete, and material enters liquid phase continous way separator, and the light phase materials in upper strata is that thick methyl esters, lower floor's heavy phase material are raw glycerine; Lower floor's heavy phase material raw glycerine, to the temporary tank of heavy phase material, starts heavy phase material discharging pump and carries out lower step neutralizing acid, separating methanol operation; The light thick methyl esters of phase materials, to the temporary tank of light phase materials, starts light phase materials discharging pump and carries out lower step separating methanol, rectification working process.
Above-mentioned is preferably embodiment of the utility model; but embodiment of the present utility model is not subject to the restriction of foregoing; other any do not deviate from change, the modification done under spirit of the present utility model and principle, substitutes, combination, simplify; all should be equivalent substitute mode, within being included in protection domain of the present utility model.
Claims (10)
1. a continuous ester interchange reactor, is characterized in that, comprises transesterification reactor and whipping appts, and wherein, the bottom of transesterification reactor is provided with compound import, and top is provided with compound outlet; In transesterification reactor, be provided with polylith dividing plate the inner chamber of transesterification reactor is separated into a plurality of cavitys; The inwall of transesterification reactor is provided with steam adjoining pipe, and the two ends of this steam adjoining pipe are respectively equipped with steam inlet and vapour outlet; Described whipping appts comprises agitator motor, stir shaft and paddle, and wherein, stir shaft is connected with agitator motor, and is arranged on from top to bottom in transesterification reactor, and described paddle is located on stir shaft.
2. continuous ester interchange reactor according to claim 1, is characterized in that, described dividing plate is three, is vertically equidistantly arranged in transesterification reactor, from top to bottom the inner chamber of transesterification reactor is divided into A, B, C, tetra-cavitys of D; Described agitator motor is arranged on the central authorities at the top of transesterification reactor; The upper end of described stir shaft is connected with agitator motor, and lower end is connected with the bearing that is located at transesterification reactor bottom, and whole stir shaft passes described dividing plate, and between stir shaft and dividing plate, has the gap of the Flow of Goods and Materials of allowing, and a paddle is set in each cavity.
3. continuous ester interchange reactor according to claim 2, is characterized in that, described compound import is arranged on the bottom centre of D cavity; Described compound outlet is arranged at the upper right corner of A cavity; Described steam inlet is arranged at the upper left corner of A cavity; Described vapour outlet is arranged at the lower right corner of D cavity.
4. continuous ester interchange reactor according to claim 3, is characterized in that, described steam adjoining pipe is spirally coiled on transesterification reactor inwall.
5. a continuous ester interchange reaction unit that comprises the continuous ester interchange reactor described in any one in claim 1～4, is characterized in that, also comprises stock oil drawing-in device, auxiliary material drawing-in device and material discharger, wherein:
Described stock oil drawing-in device comprises the temporary tank of the stock oil connecting successively, stock oil feeding pump, interchanger and stock oil flow director;
Described auxiliary material drawing-in device comprises the auxiliary material connecting successively temporary tank, auxiliary material feeding pump and auxiliary material flow director;
Described stock oil drawing-in device and auxiliary material drawing-in device are connected in parallel on mixing tank, and this mixing tank is connected with the compound import of transesterification reactor by pipeline;
Described material discharger comprises the standing separation device in the compound outlet that is connected to transesterification reactor.
6. continuous ester interchange reaction unit according to claim 5, it is characterized in that, described material discharger also comprises that light phase materials is kept in tank, gently phase materials discharging pump, heavy phase material are kept in tank and heavy phase material discharging pump, wherein, the temporary tank of described light phase materials and light phase materials discharging pump are serially connected in the top of standing separation device, and the temporary tank of described heavy phase material and heavy phase material discharging pump are serially connected in the bottom of standing separation device.
7. continuous ester interchange reaction unit according to claim 6, is characterized in that, is also connected in parallel to standby temporary tank and standby feeding volume pump on described mixing tank.
8. continuous ester interchange reaction unit according to claim 7, is characterized in that, is connected to respectively temperature regulator A and temperature regulator B on described interchanger and transesterification reactor.
9. continuous ester interchange reaction unit according to claim 8, is characterized in that, described transesterification reactor is provided with tensimeter, and this tensimeter is arranged at the top of transesterification reactor.
10. continuous ester interchange reaction unit according to claim 9, is characterized in that, on the pipeline between described compound outlet and standing separation device, is also provided with thief hole.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320457888.2U CN203474763U (en) | 2012-11-09 | 2013-07-29 | Continuous ester exchange reactor and device |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210447693 | 2012-11-09 | ||
| CN201210447693.X | 2012-11-09 | ||
| CN201320457888.2U CN203474763U (en) | 2012-11-09 | 2013-07-29 | Continuous ester exchange reactor and device |
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| Publication Number | Publication Date |
|---|---|
| CN203474763U true CN203474763U (en) | 2014-03-12 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201320457889.7U Expired - Fee Related CN203474762U (en) | 2012-11-09 | 2013-07-29 | Continuous esterification reactor and device |
| CN201320457888.2U Expired - Fee Related CN203474763U (en) | 2012-11-09 | 2013-07-29 | Continuous ester exchange reactor and device |
| CN201320457887.8U Expired - Fee Related CN203474760U (en) | 2012-11-09 | 2013-07-29 | Soapstock acidification reactor and soapstock acidification reaction device |
| CN201310323141.2A Expired - Fee Related CN103409242B (en) | 2012-11-09 | 2013-07-29 | Recycling process for alkali refining by-product, namely soapstock in refining vegetable oil and reactor |
| CN201320457890.XU Expired - Fee Related CN203474758U (en) | 2012-11-09 | 2013-07-29 | Continuous-type liquid phase separator |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201320457889.7U Expired - Fee Related CN203474762U (en) | 2012-11-09 | 2013-07-29 | Continuous esterification reactor and device |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201320457887.8U Expired - Fee Related CN203474760U (en) | 2012-11-09 | 2013-07-29 | Soapstock acidification reactor and soapstock acidification reaction device |
| CN201310323141.2A Expired - Fee Related CN103409242B (en) | 2012-11-09 | 2013-07-29 | Recycling process for alkali refining by-product, namely soapstock in refining vegetable oil and reactor |
| CN201320457890.XU Expired - Fee Related CN203474758U (en) | 2012-11-09 | 2013-07-29 | Continuous-type liquid phase separator |
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| CN203474762U (en) * | 2012-11-09 | 2014-03-12 | 广州市南洋国际工程技术服务公司 | Continuous esterification reactor and device |
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| CN100398629C (en) * | 2006-09-29 | 2008-07-02 | 合肥工业大学 | Process method for preparing biodiesel from vegetable oil soapstock |
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| CN203474762U (en) * | 2012-11-09 | 2014-03-12 | 广州市南洋国际工程技术服务公司 | Continuous esterification reactor and device |
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2013
- 2013-07-29 CN CN201320457889.7U patent/CN203474762U/en not_active Expired - Fee Related
- 2013-07-29 CN CN201320457888.2U patent/CN203474763U/en not_active Expired - Fee Related
- 2013-07-29 CN CN201320457887.8U patent/CN203474760U/en not_active Expired - Fee Related
- 2013-07-29 CN CN201310323141.2A patent/CN103409242B/en not_active Expired - Fee Related
- 2013-07-29 CN CN201320457890.XU patent/CN203474758U/en not_active Expired - Fee Related
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| CN112044389A (en) * | 2020-08-13 | 2020-12-08 | 赣州市犇牛防水建材有限公司 | Production process and equipment of waterproof coating |
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| CN113398868A (en) * | 2021-07-16 | 2021-09-17 | 浙江工业大学 | Tower type continuous flow reactor and application thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN203474762U (en) | 2014-03-12 |
| CN203474758U (en) | 2014-03-12 |
| CN103409242B (en) | 2014-11-12 |
| CN103409242A (en) | 2013-11-27 |
| CN203474760U (en) | 2014-03-12 |
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