CN201406393Y - Special device for continuously producing fatty glyceride - Google Patents
Special device for continuously producing fatty glyceride Download PDFInfo
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- CN201406393Y CN201406393Y CN200920089920XU CN200920089920U CN201406393Y CN 201406393 Y CN201406393 Y CN 201406393Y CN 200920089920X U CN200920089920X U CN 200920089920XU CN 200920089920 U CN200920089920 U CN 200920089920U CN 201406393 Y CN201406393 Y CN 201406393Y
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- esterification
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- reaction kettle
- lipid acid
- fatty acid
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Abstract
The utility model discloses a special device for continuously producing fatty glyceride. The special device comprises an esterification kettle, wherein the esterification kettle is provided with a stirrer and a bottom outlet of the esterification kettle is communicated with an inlet of a homogeneous mixing pump; an outlet of the homogeneous mixing pump is communicated with an upper inlet of the esterification kettle and provided with a finished product discharge pipe; the upper end of the esterification kettle is communicated with a vacuum system, and the upper end of the esterification kettleand/or the inlet of the homogeneous mixing pump are respectively communicated with a glycerin and catalyst filling system and an aliphatic acid filling system; and the outer wall of the esterification kettle is provided with a heating jacket, or a heating device is arranged between the homogeneous mixing pump and the esterification kettle to ensure the temperature required by the reaction. The special device can conduct complete reaction continuously, stably and automatically and improve the production efficiency, with good social and economic benefits after promotion.
Description
One, technical field:
It is that raw material carries out the equipment that the catalysis esterification reaction is produced glycerin fatty acid ester with lipid acid and glycerine that the utility model relates to a kind of, particularly relates to a kind of specific equipment of continuous production glycerin fatty acid ester.
Two, background technology:
Be raw material (fatty acid content is at 2%-100%) with lipid acid and glycerine carries out catalytic esterification when producing glycerin fatty acid ester, product is glycerin fatty acid ester and water.Traditional processing technology is that raw fatty acid and glycerine are placed in the intermittent reaction jar, stirs esterification under certain temperature and catalyzer condition.One is owing to have water generates in the reaction process, water-solublely goes in the reactant glycerine.Because esterification reaction is reversible reaction, reaction can be carried out round about, the hydrolysis reaction of glycerin fatty acid ester takes place, final esterification is carried out not exclusively, fatty acid glycerine esterification rate is lower, the purity of product glycerin fatty acid ester is low, and the fatty acid content height directly influences the use of glycerin fatty acid ester.It is two because glycerine and lipid acid objectionable intermingling, and reaction efficiency is low, thus the process of influence reaction, the numerous length of production process, energy consumption is big, and industrial production cost is high, and is extremely uneconomical.It three can only with many groups jar continuous production that form in parallel, can not realize continuous and automatic scale operation with a group jar rhythmic reaction.
Three, utility model content:
Technical problem to be solved in the utility model is: the specific equipment that is to provide a kind of continuous production glycerin fatty acid ester of continuously, stablizing, react completely, carrying out automatically.
The technical solution of the utility model is: a kind of specific equipment of continuous production glycerin fatty acid ester, contain reaction kettle of the esterification, in the described reaction kettle of the esterification agitator is installed, the outlet at bottom of described reaction kettle of the esterification is communicated with the import of intimate mixing pump, described intimate mixing pump outlet is communicated with the upper inlet of described reaction kettle of the esterification, described intimate mixing pump outlet place is provided with the finished product delivery pipe, the upper end of described reaction kettle of the esterification is communicated with vacuum system, and the ingress of the upper end of described reaction kettle of the esterification and/or described intimate mixing pump respectively with glycerine and catalyzer loading system, the lipid acid loading system is communicated with; The outer wall of described reaction kettle of the esterification is provided with heating jacket, is provided with heating unit between perhaps described intimate mixing pump and the described reaction kettle of the esterification, with the temperature that guarantees that reaction is required.
Described heating unit is spiral plate type, shell and tube or corrugated plate-type heat exchangers, and described heating jacket or heating unit are communicated with thermals source such as heat-conducting oil furnace or steam boilers respectively; The pipeline of described heating jacket or heating unit links to each other with temperature control unit with Self controlling valve, realizes the automatic control to temperature of reaction; The mixing speed of described agitator is 40-150rpm.
The finished product delivery pipe that described intimate mixing pump discharge place is provided with will react the glycerin fatty acid ester that generates directly discharges or discharges through interchanger cooling back, and described interchanger is an one-level, this interchanger and lipid acid loading system or chilled(cooling) water supply (CWS) mechanism connection; Perhaps, described interchanger is a two-stage, and its primary heat exchanger is communicated with the lipid acid loading system, its secondary heat exchanger and chilled(cooling) water supply (CWS) mechanism connection.
Described lipid acid loading system contains temporary jar of lipid acid and lipid acid transferpump, be provided with heating tube in the temporary jar of described lipid acid, this heating tube and heat-conducting oil furnace, steam boiler or finished product vent pipe are communicated with, steam, the glycerin fatty acid esters of thermal oil or generation etc. are as pre-thermal medium, and, the temporary jar lower end of described lipid acid is communicated with the import of described lipid acid transferpump, its upper end is respectively arranged with vacuum port and lipid acid inlet, described lipid acid carries pump outlet to be communicated with described reaction kettle of the esterification by described primary heat exchanger, the glycerin fatty acid ester that pre-thermal source in the primary heat exchanger generates for reaction, perhaps, described lipid acid carries pump outlet directly to be communicated with described reaction kettle of the esterification.
Glycerine and catalyzer loading system contain temporary jar of storage tank, pump and catalyzer, described storage tank is communicated with for temporary jar by described pump and described catalyzer, be provided with stirring mechanism in the temporary jar inner chamber of described catalyzer, its barrel is provided with fluid level control device, its bottom is communicated with described reaction kettle of the esterification by pump of constant delivery type, and its upper end is provided with the catalyzer inlet.
Be provided with heating tube in the described storage tank, this heating tube is communicated with heat-conducting oil furnace or steam boiler, and steam or thermal oil are as pre-thermal medium.
Be provided with liquid foam trap between described reaction kettle of the esterification and the described vacuum system, this liquid foam trap is communicated with described reaction kettle of the esterification for temporary jar by the liquid foam.
Described reaction kettle of the esterification is one, or be more than two, each described reaction kettle of the esterification and corresponding intimate mixing pump, vacuum system, heating unit, lipid acid loading system, glycerine and catalyzer loading system are formed a reaction system, the reaction kettle of the esterification of a plurality of reaction systems is connected mutually by upflow tube, the reaction kettle of the esterification of last reaction system is provided with liquid automatic control mechanism, and the feed-pipe of described lipid acid loading system is provided with flow automatic control mechanism; Perhaps, a plurality of reaction systems formula parallel with one another connects, and realizes continuous production.
The beneficial effects of the utility model are:
1, the utility model is discharged reaction kettle of the esterification by vacuum system with the water vapor that produces in the esterification, constantly be discharged from along with the resultant water vapor like this and the continuous adding of catalyzer, esterification is carried out continuously, reach transient equilibrium up to esterification, realized continuous production, enhanced productivity.
2, the utility model returns in the reaction kettle of the esterification after the homogenizing emulsifying of mixture after being mixed by the intimate mixing pump in reaction kettle of the esterification, realize circulating esterification reaction, in addition, because the special role of intimate mixing pump, make the mixture homogenizing emulsifying effective, both accelerate esterification speed, improved reactivity again, and can reach complete reaction.
3, the utility model lipid acid improves speed of response through twice preheating, and in addition, the glycerin fatty acid ester that lipid acid and reaction generate carries out heat exchange, has both reached lipid acid preheating purpose, reaches glycerin fatty acid ester cooling purpose again, kills two birds with one stone energy efficient.
4, the pipeline of the utility model heating unit links to each other with temperature control unit with Self controlling valve, realizes the automatic control to temperature of reaction.
5, the reaction kettle of the esterification of a plurality of reaction systems of the utility model is connected mutually by upflow tube, the reaction kettle of the esterification of last reaction system is provided with the liquid automatic control system, the liquid level of the reaction kettle of the esterification by controlling last reaction system automatically realizes all reaction system liquid levels controls, the lipid acid feed-pipe is provided with automatic flow control system, carry out reaction of high order, realize large scale continuous prod, and the serial connection successive reaction, cut down the consumption of energy.
6, unique, the compact construction of the utility model design, it is applied widely, has good society and economic benefit after the popularization.
Four, description of drawings:
Fig. 1 is one of the structural representation of the specific equipment of continuous production glycerin fatty acid ester;
Fig. 2 be the continuous production glycerin fatty acid ester specific equipment structural representation two.
Five, embodiment:
Embodiment one: referring to Fig. 1, among the figure, lipid acid preheating in the temporary jar V406 of lipid acid is delivered to primary heat exchanger WG402b preheating once more by lipid acid transferpump P405, delivers at last among the reaction kettle of the esterification V403a.Glycerine is transported to the temporary jar V402 of catalyzer from storage tank V401 by pump P401, simultaneously catalyzer is added among the temporary jar V402 of catalyzer to stir, and makes glycerine and catalyzer thorough mixing.The glycerine that mixing is finished joins among the reaction kettle of the esterification V403a through pump of constant delivery type P402 and reacts.Carry out for reacting fully, reaction kettle of the esterification V403a is provided with whipping appts, and stirring velocity is generally 40-150rpm.The water that reaction produces shifts out reaction system by vacuum system P406, and reaction can be carried out fully.The partial fatty acid that vacuum system is extracted out reclaims by liquid foam trap V404a, returns in the reaction kettle of the esterification by a temporary jar V405a.Lipid acid and glycerine reaction temperature are controlled at 100-250 ℃, are finished by intimate mixing pump P403a and interchanger WG401.Heating source is thermal oil or steam.Along with one of resultant water is constantly extracted out by vacuum, the continuous adding of catalyzer, reaction is constantly carried out, and lipid acid is reduced to below 10% content in reaction kettle of the esterification V403a, and reaction can reach transient equilibrium.The finished product glycerin fatty acid ester was carried storage tank stores or further processing through pump P403a after reaction was finished.Subsequent storage or add prevents that finished product glycerin fatty acid ester high temperature oxidation from arriving first among the secondary heat exchanger WG402c man-hour and cools off that cooling source is a water coolant.For improving energy utilization rate, the finished product glycerin fatty acid ester passes through primary heat exchanger WG402b in advance before cooling, carry out heat exchange with lipid acid., decolour through washing through cooling afterreaction resultant glycerin fatty acid ester, depickling, deodorization, branch is carried, and can obtain satisfactory glycerin fatty acid ester.
The proportioning of lipid acid, glycerine and catalyzer is 80-95: 5-20: 0.1-0.3, and concrete proportioning is determined according to actual needs; Catalyzer is zinc powder, SnCl
3, SnCl
4, ZnCl
2, in zinc hydroxide, sodium hydroxide and the ironic hydroxide any, choose as required, the partial fatty acid that vacuum system is extracted out reclaims by liquid foam trap V404a, returns among the reaction kettle of the esterification V403a by a temporary jar V405a again.The pipeline of interchanger WG401 links to each other with temperature control unit T401 with Self controlling valve, realizes the automatic control to temperature of reaction.Pump P401 links to each other with the liquid automatic control device H403 of the temporary jar V402 of catalyzer, realizes adding the automatic control of glycerine quantity among the temporary jar V402 of catalyzer.Be provided with heating tube among the storage tank V401, this heating tube is communicated with heat-conducting oil furnace or steam boiler, and steam or thermal oil are as pre-thermal medium.
In addition, the finished product delivery pipe that intimate mixing pump P403a exit is provided with also can directly be discharged without cooling, and perhaps, only through the first-class heat exchanger cooling, first-class heat exchanger adopts primary heat exchanger WG402b or secondary heat exchanger WG402c.Interchanger WG401 is spiral plate type, shell and tube or corrugated plate-type heat exchangers, and its thermal source is thermal oil, saturation steam or superheated vapour; Perhaps, the heating jacket on described reaction kettle of the esterification outer wall, the thermal source of this heating jacket are thermal oil, saturation steam or superheated vapour.
Be provided with heating tube among the temporary jar V406 of the lipid acid of lipid acid loading system, this heating tube is communicated with heat-conducting oil furnace, steam boiler or finished product vent pipe, the glycerin fatty acid esters of steam, thermal oil or generation etc. are as pre-thermal medium, temporary jar of V406 upper end of lipid acid is respectively arranged with vacuum port and lipid acid inlet, the outlet of lipid acid transferpump P405 can be not yet preheating and directly being communicated with once more with reaction kettle of the esterification V403a, determine as required.
Embodiment two: referring to Fig. 2, numbering is identical with embodiment one among the figure, the same meaning of representative, lipid acid is through pump P405, the glycerine that has mixed catalyzer is constantly reacted among first group of esterification system V403a of adding by pump P402, after reaching reactor V403a liquid level, flow among the next esterification system V403b by overflow spout, the liquid level of reaction kettle of the esterification V403b flows among the anti-system V403c of next esterification by overflow spout after arriving setting height, so form the series connection (among the figure be three, can adopt the serial connection of different quantities as required) of a plurality of reaction systems.Generally by last reaction system reactor (for example H402 of V403c) control liquid level, each reaction system also can be provided with liquid level control separately certainly.Placed in-line each reaction system can be carried out the control of temperature and catalyzer add-on separately.When fatty acid content changes next same reaction cycle system automatically over to when previous reaction system reaches equilibrium value.In next reaction system, increase glycerine and catalyst concentration, can make reaction continue to carry out forward, the content of reaction system lipid acid is reduced more, after a plurality of reaction system reactions, lipid acid is reduced to below 3% content in the reaction system, and reaction can finish.Whole placed in-line reaction system can be controlled total reaction times by the admission velocity of control lipid acid, feed-pipe is provided with liquid level or automatic flow control system, just can control the reaction times of total system by the flow of control lipid acid, this robot control system(RCS) can link to each other with the glycerine pump of constant delivery type P402 that has mixed catalyzer, realizes the automatic coupling of lipid acid amount and amounts of glycerol.The content that can certainly reach lipid acid in each reaction system of control by the add-on and the temperature of reaction of each reaction system glycerine of independent control, catalyzer is realized reasonably gradient of fatty acid content front and back.The entire reaction system can carry out automatically after adjusting balance, the level of automation height, and the production efficiency height can be realized large-scale continuous production.
Embodiment three: present embodiment and embodiment two are basic identical, and something in common does not repeat, and difference is: the parallel connection of a plurality of reaction systems, can adopt the parallel connection of different quantities as required, and realize large scale continuous prod.
Embodiment four: present embodiment and embodiment one or embodiment two are basic identical, something in common does not repeat, difference is: the ingress of intimate mixing pump is communicated with glycerine and catalyzer loading system, lipid acid loading system, enters reaction kettle of the esterification after the mixing again.
Embodiment five: present embodiment and embodiment one or embodiment two are basic identical, something in common does not repeat, difference is: the ingress of the upper end of reaction kettle of the esterification and intimate mixing pump is communicated with glycerine and catalyzer loading system, lipid acid loading system respectively, two place's feed.
Change each parameter concrete numerical value, change the reaction system of serial or parallel connection number, change interchanger specific constructive form, change different heating mediums, change the control mode of impelling lipid acid and the well-mixed mode of glycerine and change flow, liquid level, metering etc. and can form a plurality of embodiment, be common variation range of the present utility model, do not describe in detail one by one at this.
Claims (8)
1, a kind of specific equipment of continuous production glycerin fatty acid ester, contain reaction kettle of the esterification, in the described reaction kettle of the esterification agitator is installed, it is characterized in that: the outlet at bottom of described reaction kettle of the esterification is communicated with the import of intimate mixing pump, described intimate mixing pump outlet is communicated with the upper inlet of described reaction kettle of the esterification, described intimate mixing pump outlet place is provided with the finished product delivery pipe, the upper end of described reaction kettle of the esterification is communicated with vacuum system, and the ingress of the upper end of described reaction kettle of the esterification and/or described intimate mixing pump respectively with glycerine and catalyzer loading system, the lipid acid loading system is communicated with; The outer wall of described reaction kettle of the esterification is provided with heating jacket, is provided with heating unit between perhaps described intimate mixing pump and the described reaction kettle of the esterification, with the temperature that guarantees that reaction is required.
2, the specific equipment of continuous production glycerin fatty acid ester according to claim 1, it is characterized in that: described heating unit is spiral plate type, shell and tube or corrugated plate-type heat exchangers, and described heating jacket or heating unit are communicated with thermals source such as heat-conducting oil furnace or steam boilers respectively; The pipeline of described heating jacket or heating unit links to each other with temperature control unit with Self controlling valve, realizes the automatic control to temperature of reaction; The mixing speed of described agitator is 40-150rpm.
3, the specific equipment of continuous production glycerin fatty acid ester according to claim 1, it is characterized in that: the finished product delivery pipe that described intimate mixing pump discharge place is provided with will react the glycerin fatty acid ester that generates and directly discharge or discharge through interchanger cooling back, described interchanger is an one-level, this interchanger and lipid acid loading system or chilled(cooling) water supply (CWS) mechanism connection; Perhaps, described interchanger is a two-stage, and its primary heat exchanger is communicated with the lipid acid loading system, its secondary heat exchanger and chilled(cooling) water supply (CWS) mechanism connection.
4, the specific equipment of continuous production glycerin fatty acid ester according to claim 1, it is characterized in that: described lipid acid loading system contains temporary jar of lipid acid and lipid acid transferpump, be provided with heating tube in the temporary jar of described lipid acid, this heating tube and heat-conducting oil furnace, steam boiler or finished product vent pipe are communicated with, steam, the glycerin fatty acid esters of thermal oil or generation etc. are as pre-thermal medium, and, the temporary jar lower end of described lipid acid is communicated with the import of described lipid acid transferpump, its upper end is respectively arranged with vacuum port and lipid acid inlet, described lipid acid carries pump outlet to be communicated with described reaction kettle of the esterification by described primary heat exchanger, the glycerin fatty acid ester that pre-thermal source in the primary heat exchanger generates for reaction, perhaps, described lipid acid carries pump outlet directly to be communicated with described reaction kettle of the esterification.
5, the specific equipment of continuous production glycerin fatty acid ester according to claim 1, it is characterized in that: glycerine and catalyzer loading system contain temporary jar of storage tank, pump and catalyzer, described storage tank is communicated with for temporary jar by described pump and described catalyzer, be provided with stirring mechanism in the temporary jar inner chamber of described catalyzer, its barrel is provided with fluid level control device, its bottom is communicated with described reaction kettle of the esterification by pump of constant delivery type, and its upper end is provided with the catalyzer inlet.
6, the specific equipment of continuous production glycerin fatty acid ester according to claim 5 is characterized in that: be provided with heating tube in the described storage tank, this heating tube is communicated with heat-conducting oil furnace or steam boiler, and steam or thermal oil are as pre-thermal medium.
7, the specific equipment of continuous production glycerin fatty acid ester according to claim 1, it is characterized in that: be provided with liquid foam trap between described reaction kettle of the esterification and the described vacuum system, this liquid foam trap is communicated with described reaction kettle of the esterification for temporary jar by the liquid foam.
8, specific equipment according to the arbitrary described continuous production glycerin fatty acid ester of claim 1-7, it is characterized in that: described reaction kettle of the esterification is one, or be more than two, each described reaction kettle of the esterification and corresponding intimate mixing pump, vacuum system, heating unit, the lipid acid loading system, glycerine and catalyzer loading system are formed a reaction system, the reaction kettle of the esterification of a plurality of reaction systems is connected mutually by upflow tube, the reaction kettle of the esterification of last reaction system is provided with liquid automatic control mechanism, and the feed-pipe of described lipid acid loading system is provided with flow automatic control mechanism; Perhaps, a plurality of reaction systems formula parallel with one another connects, and realizes continuous production.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200920089920XU CN201406393Y (en) | 2009-04-29 | 2009-04-29 | Special device for continuously producing fatty glyceride |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200920089920XU CN201406393Y (en) | 2009-04-29 | 2009-04-29 | Special device for continuously producing fatty glyceride |
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| CN201406393Y true CN201406393Y (en) | 2010-02-17 |
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| CN200920089920XU Expired - Lifetime CN201406393Y (en) | 2009-04-29 | 2009-04-29 | Special device for continuously producing fatty glyceride |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102417865A (en) * | 2010-09-28 | 2012-04-18 | 江苏中鼎化学有限公司 | Method for continuously producing mono-and-di-glyceride |
| CN101575285B (en) * | 2009-04-29 | 2013-07-17 | 李普选 | Technical method for continuously producing fatty glyceride and special equipment thereof |
| CN108330001A (en) * | 2018-04-25 | 2018-07-27 | 浙江工业大学 | A kind of serialization glycerine esterification deacidification device |
-
2009
- 2009-04-29 CN CN200920089920XU patent/CN201406393Y/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101575285B (en) * | 2009-04-29 | 2013-07-17 | 李普选 | Technical method for continuously producing fatty glyceride and special equipment thereof |
| CN102417865A (en) * | 2010-09-28 | 2012-04-18 | 江苏中鼎化学有限公司 | Method for continuously producing mono-and-di-glyceride |
| CN102417865B (en) * | 2010-09-28 | 2013-08-28 | 江苏中鼎化学有限公司 | Method for continuously producing mono-and-di-glyceride |
| CN108330001A (en) * | 2018-04-25 | 2018-07-27 | 浙江工业大学 | A kind of serialization glycerine esterification deacidification device |
| CN108330001B (en) * | 2018-04-25 | 2019-03-29 | 浙江工业大学 | A kind of serialization glycerine esterification deacidification device |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20100217 Effective date of abandoning: 20090429 |
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| RGAV | Abandon patent right to avoid regrant |