CN205275489U - Produce separator of glycerine and methyl alcohol in biodiesel technology - Google Patents
Produce separator of glycerine and methyl alcohol in biodiesel technology Download PDFInfo
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- CN205275489U CN205275489U CN201620001740.1U CN201620001740U CN205275489U CN 205275489 U CN205275489 U CN 205275489U CN 201620001740 U CN201620001740 U CN 201620001740U CN 205275489 U CN205275489 U CN 205275489U
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- glycerine
- methyl alcohol
- dealcoholize column
- dealcoholize
- liquid
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Abstract
The utility model discloses a produce separator of glycerine and methyl alcohol in biodiesel technology. The device includes raw materials conveying system, first separation system and secondary separation system, raw materials conveying system comprises delivery pump and heater. The first separation system is the dealcoholize tower of tower cauldron formula structure, and inside is equipped with the spiral nozzle and keeps off the liquid awl with the reflection for carry out the first separation, and with the leading -in secondary separation system of the methyl alcohol vapour of after -separating, the secondary separation system hydrocyclone be, with the methyl alcohol vapour derivation of isolating, the glycerine first separation system that flows back will be isolated. Utilize the poor big characteristics of boiling point of glycerine, methyl alcohol, two kinds of components in the mixed liquid of glycerine - methyl alcohol of the vaporific attitude of loseing one's temper are vaporized respectively and are liquefied, carry out two -stage separation with methyl alcohol again, make glycerine and methyl alcohol carry out the mass transfer heat transfer effect twice in the dealcoholize tower, make glycerine and methyl alcohol separate. The utility model has the advantages of difficult jam, low, the after -separating purity height of energy consumption.
Description
Technical field
The utility model belongs to technical field of chemical, is specifically related to produce in a kind of biodiesel processes the tripping device of glycerine and methyl alcohol.
Background technology
Biofuel is taking Vegetable oil lipoprotein and animal grease etc. such as oil crops, Wild oil plant, micro-algaes as stock oil, with the fuel of the replaced petrifaction diesel that alcohol class is made by ester exchange process, is a kind of eco-friendly renewable energy source. The method for producing biodiesel that industry is commonly used has the alcoholysis method of low acid value grease, the esterification of soda acid two-stage catalysis to add alcoholysis method, no matter which kind of method, in grease and alcohol (mainly methyl alcohol) reaction process except generating fatty acid ester (biofuel), also can generate a large amount of by-product glycerins.
In current production process, generally use excessive methyl alcohol, and glycerine and methyl alcohol mutually dissolve, so being difficult to separation by general settlement separate mode. Therefore the practice usually taked now is: is first all by methyl alcohol and glycerol mixture collection by glycerine and separating methanol, then adopts rectifying separation. The equipment manufacturing cost height that this kind of separate mode not only uses, and glycerine very easily cause during rectifying in tower filler or column plate blocking. In addition, owing to glycerine and methyl alcohol dissolve each other, it is necessary to very big reflux ratio just can carry out rectifying, causes separating energy consumption height, processing power more weak.
Blocking when how to solve glycerine and separating methanol, reducing energy consumption is this area problem demanding prompt solution.
Practical novel content
For prior art above shortcomings, the biodiesel processes that the purpose of this utility model is to provide a kind of not easily blocking, energy consumption is low, separation after product purity is high produces the tripping device of glycerine and methyl alcohol.
In order to realize above-mentioned purpose, the technical solution adopted in the utility model is as follows:
Biodiesel processes produces a tripping device for glycerine and methyl alcohol, comprises source material delivery system, flash liberation system and secondary separating system; Described source material delivery system comprises take away pump and well heater, and described take away pump is connected with the opening for feed of described well heater, the discharge port of described well heater and flash liberation system connectivity; Described flash liberation system is the dealcoholize column of tower reactor formula structure; One end of the feed-pipe of this dealcoholize column is connected with the discharge port of described well heater, the other end is the spiral nozzle being positioned at dealcoholize column inner chamber top, this spiral nozzle is positioned on the axis of described dealcoholize column, for being sprayed in aerosol form in dealcoholize column by glycerine-methyl alcohol mixed liquor; The top of described dealcoholize column is provided with a separating methanol pipe, for the methyl alcohol that flash liberation systematic position goes out is transported to secondary separating system; The bottom of described dealcoholize column is provided with glycerine output tube, for by the dealcoholize column described in liquid glycerin discharge; Being provided with reflection gear liquid cone between described spiral nozzle and described separating methanol pipe, this reflection gear liquid cone is the cone of lower ending opening, for the glycerin component retained in steam; Described secondary separating system is wet cyclone, is connected with described separating methanol pipe in the middle part of this wet cyclone, and top is provided with two separating methanol pipes for discharging methyl alcohol, and bottom is provided with two glycerine return lines; These two glycerine return lines are connected with described dealcoholize column, are back in dealcoholize column for the glycerine isolated by wet cyclone.
Further, also comprising the glycerine recycle system, the described glycerine recycle system comprises recycle pump and reboiler; Described glycerine output tube is connected with described recycle pump, and described recycle pump is connected by glycerine circulation tube with the fluid inlet of described reboiler; The liquid outlet of described reboiler is connected with the circulation glycerine import of described dealcoholize column; Described circulation glycerine import is positioned at below described spiral nozzle; Described glycerine circulation tube is provided with glycerine recovery tube.
Further, also it is provided with in described dealcoholize column and the liquid distributor that its internal diameter mates mutually; Described liquid distributor keeps off in described reflection between liquid cone and spiral nozzle, and is connected with described two glycerine return lines.
Further, described dealcoholize column is provided with sight glass, for observing the response situation of dealcoholize column inside.
Further, described glycerine output tube, glycerine circulation tube and glycerine recovery tube are provided with valve.
Further, described well heater and reboiler are tube-sheet heat exchanger; The upper and lower part of described well heater is provided with heating medium respectively and imports and exports; The upper and lower part of described reboiler is provided with the medium that boils again respectively and imports and exports.
Further, being also provided with structured packing between described circulation glycerine import and described spiral nozzle, the internal diameter of this structured packing and described dealcoholize column adapts.
Compared with prior art, the utility model has following useful effect:
1, the utility model will be heated to the glycerine of certain temperature, methanol mixed material and be substantially increased by the atomizing of spiral nozzle the specific surface area of liquid, utilize the principle that methyl alcohol and glycerine boiling point differ greatly, make methyl alcohol fast vaporizing so that it is separate from glycerine.
2, realize twice glycerine in the utility model dealcoholize column continuously, the heat and mass transfer of methyl alcohol exchanges, it is to increase the glycerine separated and the purity of methyl alcohol. The utility model utilizes gear liquid cone and wet cyclone to combine, and solves methyl alcohol evaporation glycerine entrainment problem. Utilize boiling-point difference, adopt gear liquid cone to be deviate from gas-phase methanol by glycerine for twice with wet cyclone, it is to increase the concentration of gas-phase methanol product.
3, the utility model utilizes reboiler, makes the glycerine bottom dealcoholize column and the methyl alcohol vaporizing in Trace Methanol, enters gas phase in tower, takes off except the methyl alcohol in glycerine extremely goodly.
4, the utility model will adopt vacuum system, methyl alcohol (boiling point 64.7 DEG C) is utilized to be separated with glycerine (290 DEG C) feature that boiling point difference is big, guarantee glycerine can not be polymerized with decompose while, saved the energy to maximum degree, its energy-output ratio only have rectifying tower about 2/5.
5, without any column plate in the utility model, operate continuously at a certain temperature, not easily blocks.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model.
In accompanying drawing: 11 take away pumps; 12 well heaters; 121 heating mediums are imported and exported; 2 dealcoholize columns; 21 spiral nozzles; 22 reflection gear liquid cones; 23 liquid distributors; 24 sight glasss; 25 separating methanol pipes; 26 glycerine output tubes; 27 circulation glycerine imports; 28 structured packings; 3 wet cyclones; 31 2 separating methanol pipes; 32 2 glycerine return lines; 41 recycle pumps; 42 reboilers; 421 boil again medium import and export; 43 glycerine circulation tubes; 44 glycerine recovery tube.
Embodiment
Below in conjunction with specific embodiment, the utility model is described in further detail.
Biodiesel processes produces a tripping device for glycerine and methyl alcohol, comprises source material delivery system, flash liberation system and secondary separating system:
Described source material delivery system comprises take away pump 11 and well heater 12, and described take away pump 11 is connected with the opening for feed of described well heater 12, the discharge port of described well heater 12 and flash liberation system connectivity.
Described flash liberation system is the dealcoholize column 2 of tower reactor formula structure; One end of the feed-pipe of this dealcoholize column 2 is connected with the discharge port of described well heater 12, the other end is the spiral nozzle 21 being positioned at dealcoholize column 2 inner chamber top, this spiral nozzle 21 is positioned on the axis of described dealcoholize column 2, for being sprayed in dealcoholize column 2 in aerosol form by glycerine-methyl alcohol mixed liquor; The top of described dealcoholize column 2 is provided with a separating methanol pipe 25, for the methyl alcohol that flash liberation systematic position goes out is transported to secondary separating system; The bottom of described dealcoholize column 2 is provided with glycerine output tube 26, for by the dealcoholize column 2 described in liquid glycerin discharge; Being provided with reflection gear liquid cone 22 between described spiral nozzle 21 and described separating methanol pipe 25, this reflection gear liquid cone 22 is the cone of lower ending opening, for the glycerin component retained in steam. Spiral nozzle 21 select it is ensured that the diameter in spray liquid face formed is identical with tower hypomere diameter, to ensure that atomization is in optimum regime.
Described secondary separating system is wet cyclone 3, is connected with described separating methanol pipe 25 in the middle part of this wet cyclone 3, and top is provided with two separating methanol pipes 31 for discharging methyl alcohol, and bottom is provided with two glycerine return lines 32; These two glycerine return lines 32 are connected with described dealcoholize column 2, for being back in dealcoholize column 2 by the glycerine that wet cyclone 3 is isolated.
As one preferred embodiment, this device can also be provided with the glycerine recycle system, and the described glycerine recycle system comprises recycle pump 41 and reboiler 42; Described glycerine output tube 26 is connected with described recycle pump 41, and described recycle pump 41 is connected by glycerine circulation tube 43 with the fluid inlet of described reboiler 42; The liquid outlet of described reboiler 42 is connected with the circulation glycerine import 27 of described dealcoholize column 2; Described circulation glycerine import 27 is positioned at below described spiral nozzle 21; Described glycerine circulation tube 43 is provided with glycerine recovery tube 44.
As one preferred embodiment, the liquid distributor 23 mated mutually with its internal diameter also it is provided with in described dealcoholize column 2; Described liquid distributor 23 keeps off in described reflection between liquid cone 22 and spiral nozzle 21, and is connected with described two glycerine return lines 32.
As one preferred embodiment, described dealcoholize column 2 is provided with sight glass 24, for observing the response situation of dealcoholize column 2 inside.
As one preferred embodiment, described glycerine output tube 26, glycerine circulation tube 43 and glycerine recovery tube 44 are provided with valve. Flow, flow velocity can be regulated by the valve on glycerine output tube 26, glycerine circulation tube 43; By opening glycerine recovery tube 44, glycerine qualified for composition can also be added and receives in storage.
As one preferred embodiment, described well heater 12 and reboiler 42 are tube-sheet heat exchanger; The upper and lower part of described well heater 12 is provided with heating medium respectively and imports and exports 121; The upper and lower part of described reboiler 42 is provided with the medium that boils again respectively and imports and exports 421. Heating medium and the medium that boils again can use gaseous medium (such as water vapour), it is possible to use liquid medium (such as thermal oil). Adopt gaseous medium then to adopt the mode of upper entering and lower leaving to heat, adopt liquid medium then to adopt the mode of bottom in and top out to heat, to ensure that heating medium has enough dead time in shell side.
As one preferred embodiment, being also provided with structured packing 28 between described circulation glycerine import 27 and described spiral nozzle 21, this structured packing 28 adapts with the internal diameter of described dealcoholize column 2.
In actual use, operate according to the following steps:
1) first enter in well heater to heat by preparing in biodiesel process the glycerine-methanol mixed liquid pump produced, then it to be drenched by spiral nozzle spray be the top of dealcoholize column of-0.06��0.07MPa in vacuum tightness, to form the spraying of 80 DEG C��90 DEG C; Under making the effect that this is sprayed at temperature and vacuum, form a steam of gas phase and the sedimentation liquid of liquid phase; Make a described steam through reflection gear liquid cone again, allow part component wherein be formed and retain liquid; Described sedimentation liquid, retain liquid and all form dripping drops.
Main component in a steam is carry the methyl alcohol of a small amount of glycerin component secretly, and sedimentation liquid is then for having carried the glycerine of a small amount of methyl alcohol component secretly. Steam runs into reflection gear liquid cone in rising, and glycerin component wherein can be retained down and become liquid state and retain liquid, and the glycerol content in a steam is greatly reduced, and sedimentation liquid and retain liquid and can fall under gravity.
2) it is separated step 1) imports wet cyclone through a steam of reflection gear liquid cone, obtains two steams of gas phase and the phegma of liquid phase; Again two steams are discharged to methanol recovery device, phegma is back to dealcoholize column; Make phegma form drop to contact with a steam of rising, form backflow drop;
Two steams are the methyl alcohol of purity >=99.5%, and phegma is then for having carried the glycerine of Trace Methanol secretly. Phegma contacts with a steam with the form of drop, and mass-and heat-transfer effect occurs, and namely phegma makes a small amount of glycerine steam in steam liquefy, and forms the backflow drop of whereabouts, and the heat of phegma makes methyl alcohol vaporizing rise together with phegma.
3) by the dripping drops in step 1) and step 2) in phegma drop in and bottom dealcoholize column, accumulate sedimentation liquid, and discharged.
4) the sedimentation liquor pump of discharge is entered reboiler, make it to be formed circulation steam and the circulation fluid of 140 DEG C, and be transported to the top of dealcoholize column, the lower section of spiral nozzle; Make in the structured packing that the circulation steam upwards moved enters in dealcoholize column, and with above structured packing, enter backflow drop wherein contact with dripping drops; Circulation fluid then moves downward and enters sedimentation liquid.
Sedimentation liquid is the glycerine being entrained with a small amount of methyl alcohol component, is controlled by drop temperature in reboiler at about 140 DEG C, the temperature far below glycerol polymerization decomposition, the boiling point higher than methyl alcohol. By the heating of reboiler so that it is in methyl alcohol composition turn into circulation steam, glycerin component and then occur with the form of the circulation fluid of liquid state. The liquid of circulation steam and whereabouts enters structured packing generation mass-and heat-transfer effect from upper and lower respectively, and the methyl alcohol component in the two forms steam rising under the effect of heat, glycerin component forms droplets fall. Circulation fluid then enters in sedimentation liquid.
5) repeating step 1)-4), said process circulation is occurred, checks the component of sedimentation liquid in good time, when its methanol content��0.5%, derived glycerine retrieving arrangement.
Methanol content >=99.5% that the utility model is separated, meets the requirement of production of biodiesel methanol content completely; And steam, electricity equal energy source consumption only rectifying tower 2/5; The glycerine separated detects through assay, and wherein methanol content is below 0.5%, for next step process of glycerine is laid a good foundation.
The utility model has carried out three grades based on methyl alcohol from the temperature head of the boiling point of glycerine and has been separated: the first step is spiral nozzle glycerine-methyl alcohol mixed liquor out owing to boiling point is different and make a large amount of methyl alcohol vaporizing, glycerine liquefy; The second stage be wet cyclone by a large amount of separating methanol out, then will be that the phegma of main ingredient again enters dealcoholize column by liquid distributor and makes it to contact with a steam mass-and heat-transfer effect occurs taking glycerine; The third stage is then allow the liquid of circulation steam and whereabouts enter structured packing generation mass-and heat-transfer effect from upper and lower respectively.
Above-described embodiment of the present utility model is only for the utility model example is described, and is not the restriction to enforcement mode of the present utility model. For those of ordinary skill in the field, other multi-form change and variations can also be made on the basis of the above description. Here cannot all enforcement modes be given exhaustive. Every belong to apparent change that the technical solution of the utility model amplified out or variation is still in the row of protection domain of the present utility model.
Claims (7)
1. a biodiesel processes produces the tripping device of glycerine and methyl alcohol, it is characterised in that, comprise source material delivery system, flash liberation system and secondary separating system;
Described source material delivery system comprises take away pump and well heater, and described take away pump is connected with the opening for feed of described well heater, the discharge port of described well heater and flash liberation system connectivity;
Described flash liberation system is the dealcoholize column of tower reactor formula structure; One end of the feed-pipe of this dealcoholize column is connected with the discharge port of described well heater, the other end is the spiral nozzle being positioned at dealcoholize column inner chamber top, this spiral nozzle is positioned on the axis of described dealcoholize column, for being sprayed in aerosol form in dealcoholize column by glycerine-methyl alcohol mixed liquor; The top of described dealcoholize column is provided with a separating methanol pipe, for the methyl alcohol that flash liberation systematic position goes out is transported to secondary separating system; The bottom of described dealcoholize column is provided with glycerine output tube, for by the dealcoholize column described in liquid glycerin discharge; Being provided with reflection gear liquid cone between described spiral nozzle and described separating methanol pipe, this reflection gear liquid cone is the cone of lower ending opening, for the glycerin component retained in steam;
Described secondary separating system is wet cyclone, is connected with described separating methanol pipe in the middle part of this wet cyclone, and top is provided with two separating methanol pipes for discharging methyl alcohol, and bottom is provided with two glycerine return lines; These two glycerine return lines are connected with described dealcoholize column, are back in dealcoholize column for the glycerine isolated by wet cyclone.
2. biodiesel processes according to claim 1 produces the tripping device of glycerine and methyl alcohol, it is characterised in that, also comprise the glycerine recycle system, the described glycerine recycle system comprises recycle pump and reboiler; Described glycerine output tube is connected with described recycle pump, and described recycle pump is connected by glycerine circulation tube with the fluid inlet of described reboiler; The liquid outlet of described reboiler is connected with the circulation glycerine import of described dealcoholize column; Described circulation glycerine import is positioned at below described spiral nozzle; Described glycerine circulation tube is provided with glycerine recovery tube.
3. biodiesel processes according to claim 1 produces the tripping device of glycerine and methyl alcohol, it is characterised in that, also it is provided with in described dealcoholize column and the liquid distributor that its internal diameter mates mutually; Described liquid distributor keeps off in described reflection between liquid cone and spiral nozzle, and is connected with described two glycerine return lines.
4. biodiesel processes according to claim 1 produces the tripping device of glycerine and methyl alcohol, it is characterised in that, described dealcoholize column is provided with sight glass, for observing the response situation of dealcoholize column inside.
5. biodiesel processes according to claim 2 produces the tripping device of glycerine and methyl alcohol, it is characterised in that, described glycerine output tube, glycerine circulation tube and glycerine recovery tube are provided with valve.
6. biodiesel processes according to claim 2 produces the tripping device of glycerine and methyl alcohol, it is characterised in that, described well heater and reboiler are tube-sheet heat exchanger; The upper and lower part of described well heater is provided with heating medium respectively and imports and exports; The upper and lower part of described reboiler is provided with the medium that boils again respectively and imports and exports.
7. biodiesel processes according to claim 2 produces the tripping device of glycerine and methyl alcohol, it is characterized in that, also being provided with structured packing between described circulation glycerine import and described spiral nozzle, the internal diameter of this structured packing and described dealcoholize column adapts.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620001740.1U CN205275489U (en) | 2016-01-04 | 2016-01-04 | Produce separator of glycerine and methyl alcohol in biodiesel technology |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620001740.1U CN205275489U (en) | 2016-01-04 | 2016-01-04 | Produce separator of glycerine and methyl alcohol in biodiesel technology |
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| CN205275489U true CN205275489U (en) | 2016-06-01 |
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| CN201620001740.1U Expired - Fee Related CN205275489U (en) | 2016-01-04 | 2016-01-04 | Produce separator of glycerine and methyl alcohol in biodiesel technology |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105418369A (en) * | 2016-01-04 | 2016-03-23 | 重庆浩泰能源有限公司 | Separating device and method for glycerinum and methyl alcohol produced in biodiesel technology |
-
2016
- 2016-01-04 CN CN201620001740.1U patent/CN205275489U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105418369A (en) * | 2016-01-04 | 2016-03-23 | 重庆浩泰能源有限公司 | Separating device and method for glycerinum and methyl alcohol produced in biodiesel technology |
| CN105418369B (en) * | 2016-01-04 | 2017-06-16 | 重庆浩泰能源有限公司 | The separator and method of glycerine and methyl alcohol are produced in a kind of biodiesel processes |
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Legal Events
| 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: 20160601 Termination date: 20190104 |