CN101575285A - Technical method for continuously producing fatty glyceride and special equipment thereof - Google Patents
Technical method for continuously producing fatty glyceride and special equipment thereof Download PDFInfo
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- CN101575285A CN101575285A CN 200910064750 CN200910064750A CN101575285A CN 101575285 A CN101575285 A CN 101575285A CN 200910064750 CN200910064750 CN 200910064750 CN 200910064750 A CN200910064750 A CN 200910064750A CN 101575285 A CN101575285 A CN 101575285A
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Abstract
The invention discloses a technical method for continuously producing fatty glyceride and special equipment thereof. The technical method comprises the steps of: adding a fatty acid, glycerin and a catalyst to an esterification reaction kettle and allowing the mixture to enter into a homogeneous blending pump for homogeneous emulsion after stirring, realizing circular esterification reaction after the mixture passing through the homogeneous blending pump enters the upper part of the esterification reaction kettle, heating through a heating device in the esterification reaction, discharging the water vapor generated in the esterification reaction kettle through a vacuum system, and continuously conducting the esterification reaction along with the water vapor discharged constantly and the catalyst added constantly until the end of the esterification reaction. The bottom of the esterification reaction kettle of the special equipment is communicated with the upper part thereof through the homogeneous blending pump, the outlet of which is provided with a finished product discharge pipe. The external wall of the esterification reaction kettle is provided with a heating jacket, or the heating device is arranged between the homogeneous blending pump and the esterification reaction kettle. The invention can be continuously, stably and automatically conducted with complete reaction and good economic benefit.
Description
One, technical field:
The present invention relates to a kind of is that raw material carries out processing method and the equipment that the catalysis esterification reaction is produced glycerin fatty acid ester with lipid acid and glycerine, particularly relates to a kind of processing method and specific equipment thereof 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, summary of the invention:
Technical problem to be solved by this invention is: the processing method and the specific equipment thereof that are to provide a kind of continuous production glycerin fatty acid ester of continuously, stablizing, react completely, carrying out automatically.
Technical scheme of the present invention is: a kind of processing method of continuous production glycerin fatty acid ester, comprise: with lipid acid, glycerine and catalyst by proportion join in the reaction kettle of the esterification, stir by agitator, the outlet at bottom of mixture after being mixed by reaction kettle of the esterification enters and carries out homogenizing emulsifying in the intimate mixing pump, with enhance esterification speed, enter the top of reaction kettle of the esterification through the mixture of intimate mixing pump, realize circulating esterification reaction, in esterification reaction process, mixture is heated by heating unit, the water vapor that produces in the esterification is discharged reaction kettle of the esterification by vacuum system, along with the resultant water vapor constantly is discharged from and the continuous adding of catalyzer, esterification is carried out continuously, reaches transient equilibrium up to esterification.
The proportioning of described lipid acid, glycerine and catalyzer is 80-95: 5-20: 0.1-0.3; The temperature of described esterification is 100-250 ℃, and the mixing speed of described agitator is 40-150rpm, and described catalyzer is zinc powder, SnCl
3, SnCl
4, ZnCl
2, zinc hydroxide, sodium hydroxide or ironic hydroxide, lipid acid is reduced to 10% content when following in the described reaction kettle of the esterification, esterification reaches running balance, the glycerin fatty acid ester that reaction generates is directly discharged or is discharged through interchanger cooling back, the glycerin fatty acid ester of discharging is washed again, decolouring, depickling, deodorization, branch are carried, and can obtain satisfactory glycerin fatty acid ester; Described interchanger is an one-level, and the cooling source of this interchanger is vegetable fatty acids or a water coolant to be added; Perhaps, described interchanger is a two-stage, and the cooling source of the primary heat exchanger of described two-stage interchanger is a vegetable fatty acids to be added, and the cooling source of its secondary heat exchanger is a water coolant.
Described heating unit is spiral plate type, shell and tube or corrugated plate-type heat exchangers, enter the top of described reaction kettle of the esterification after the mixture of the described intimate mixing pump of process heats by described heating unit, the thermal source of described heating unit is thermal oil, saturation steam or superheated vapour; Perhaps, described heating unit is the heating jacket that is arranged on the described reaction kettle of the esterification outer wall, and the thermal source of this heating jacket is thermal oil, saturation steam or superheated vapour; The pipeline of described heating unit links to each other with temperature control unit with Self controlling valve, realizes the automatic control to temperature of reaction.
With lipid acid preheating in the temporary jar of lipid acid, pre-thermal source is the glycerin fatty acid ester that steam, thermal oil or esterification generate, vegetable fatty acids through preheating is transported in the reaction kettle of the esterification by the lipid acid transferpump, perhaps be transported to preheating once more in the described primary heat exchanger, deliver in the described reaction kettle of the esterification glycerin fatty acid ester that the pre-thermal source in the primary heat exchanger generates for reaction then; Glycerine is kept in the jar to catalyzer by pump delivery from storage tank, simultaneously catalyzer is added in the temporary jar of catalyzer and stir by agitator, make glycerine and catalyzer thorough mixing, mixed glycerine and catalyzer join in the described reaction kettle of the esterification through pump of constant delivery type, glycerine and lipid acid carry out quick esterification under the effect of catalyzer, perhaps, lipid acid and glycerine and catalyzer are sent into earlier to send in the reaction kettle of the esterification behind the thorough mixing in the intimate mixing pump again and are reacted, perhaps, lipid acid and glycerine and catalyzer a part simultaneously advance reactor, a part is advanced the intimate mixing pump, carries out esterification.
The partial fatty acid that described vacuum system is extracted out reclaims by liquid foam trap, returns in the described reaction kettle of the esterification by temporary jar again.
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, fatty acid glycerine and catalyzer adding system form 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 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, adjust lipid acid, the proportioning of glycerine and catalyzer, carry out reaction of high order, lipid acid is reduced to below 10% content in last reaction system, and esterification reaches transient equilibrium; Perhaps, a plurality of reaction systems formula parallel with one another connects, and realizes continuous production.
A kind of specific equipment of processing method of described 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, and the finished product delivery pipe that described intimate mixing pump discharge place is provided with is communicated with interchanger, and this interchanger is an one-level, this interchanger and lipid acid loading system or chilled(cooling) water supply (CWS) mechanism connection; Perhaps, this 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, be provided with heating tube in the described storage tank, this heating tube is communicated with heat-conducting oil furnace or steam boiler, steam or thermal oil are as pre-thermal medium, described storage tank is communicated with for temporary jar by described pump and described catalyzer, is provided with stirring mechanism in the temporary jar inner chamber of described catalyzer, and 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 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 invention has the beneficial effects as follows:
1, the present invention discharges reaction kettle of the esterification by vacuum system with the water vapor that produces in the esterification, constantly be discharged from along with water vapor like this and the continuous adding of catalyzer, esterification is carried out continuously, finishes up to esterification, realized continuous production, enhanced productivity.
2, the present invention 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, lipid acid of the present invention 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 heating unit of the present invention 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 present invention 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, technology uniqueness of the present invention, equipment advanced person, it is applied widely, has good society and economic benefit after the popularization.
Four, description of drawings:
Fig. 1 is one of structural representation of specific equipment of the present invention;
Fig. 2 is two of the structural representation of specific equipment of the present invention.
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, wherein, lipid acid can choose 80,82,85,88,90,92,95 etc., glycerine can choose 5,8,10,12,15,18,20 etc., catalyzer can choose 0.1,0.15,0.2,0.25,0.3 etc., 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 invention, do not describe in detail one by one at this.
Claims (10)
1, a kind of processing method of continuous production glycerin fatty acid ester, it is characterized in that: with lipid acid, glycerine and catalyst by proportion join in the reaction kettle of the esterification, stir by agitator, the outlet at bottom of mixture after being mixed by reaction kettle of the esterification enters and carries out homogenizing emulsifying in the intimate mixing pump, with enhance esterification speed, enter the top of reaction kettle of the esterification through the mixture of intimate mixing pump, realize circulating esterification reaction, in esterification reaction process, mixture is heated by heating unit, the water vapor that produces in the esterification is discharged reaction kettle of the esterification by vacuum system, along with the resultant water vapor constantly is discharged from and the continuous adding of catalyzer, esterification is carried out continuously, reaches transient equilibrium up to esterification.
2, the processing method of continuous production glycerin fatty acid ester according to claim 1 is characterized in that: the proportioning of described lipid acid, glycerine and catalyzer is 80-95: 5-20: 0.1-0.3; The temperature of described esterification is 100-250 ℃, and the mixing speed of described agitator is 40-150rpm, and described catalyzer is zinc powder, SnCl
3, SnCl
4, ZnCl
2, in zinc hydroxide, sodium hydroxide and the ironic hydroxide any, lipid acid is reduced to 10% content when following in the described reaction kettle of the esterification, esterification reaches running balance, the glycerin fatty acid ester that reaction generates is directly discharged or is discharged through interchanger cooling back, the glycerin fatty acid ester of discharging is washed again, decolouring, depickling, deodorization, branch are carried, and can obtain satisfactory glycerin fatty acid ester; Described interchanger is an one-level, and the cooling source of this interchanger is vegetable fatty acids or a water coolant to be added; Perhaps, described interchanger is a two-stage, and the cooling source of the primary heat exchanger of described two-stage interchanger is a vegetable fatty acids to be added, and the cooling source of its secondary heat exchanger is a water coolant.
3, the processing method of continuous production glycerin fatty acid ester according to claim 2, it is characterized in that: described heating unit is spiral plate type, shell and tube or corrugated plate-type heat exchangers, enter the top of described reaction kettle of the esterification after the mixture of the described intimate mixing pump of process heats by described heating unit, the thermal source of described heating unit is thermal oil, saturation steam or superheated vapour; Perhaps, described heating unit is the heating jacket that is arranged on the described reaction kettle of the esterification outer wall, and the thermal source of this heating jacket is thermal oil, saturation steam or superheated vapour; The pipeline of described heating unit links to each other with temperature control unit with Self controlling valve, realizes the automatic control to temperature of reaction.
4, the processing method of continuous production glycerin fatty acid ester according to claim 3, it is characterized in that: with lipid acid preheating in the temporary jar of lipid acid, pre-thermal source is the glycerin fatty acid ester that steam, thermal oil or esterification generate, vegetable fatty acids through preheating is transported in the reaction kettle of the esterification by the lipid acid transferpump, perhaps be transported to preheating once more in the described primary heat exchanger, deliver in the described reaction kettle of the esterification glycerin fatty acid ester that the pre-thermal source in the primary heat exchanger generates for reaction then; Glycerine is kept in the jar to catalyzer by pump delivery from storage tank, simultaneously catalyzer is added in the temporary jar of catalyzer and stir by agitator, make glycerine and catalyzer thorough mixing, mixed glycerine and catalyzer join in the described reaction kettle of the esterification through pump of constant delivery type, glycerine and lipid acid carry out quick esterification under the effect of catalyzer, perhaps, lipid acid and glycerine and catalyzer are sent into earlier to send in the reaction kettle of the esterification behind the thorough mixing in the intimate mixing pump again and are reacted, perhaps, lipid acid and glycerine and catalyzer a part simultaneously advance reactor, a part is advanced the intimate mixing pump, carries out esterification.
5, the processing method of continuous production glycerin fatty acid ester according to claim 4 is characterized in that: the partial fatty acid that described vacuum system is extracted out reclaims by liquid foam trap, returns in the described reaction kettle of the esterification by temporary jar again.
6, processing method according to the arbitrary described continuous production glycerin fatty acid ester of claim 1-5, 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, fatty acid glycerine and catalyzer adding system form 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 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, adjust lipid acid, the proportioning of glycerine and catalyzer, carry out reaction of high order, lipid acid is reduced to below 10% content in last reaction system, and esterification reaches transient equilibrium; Perhaps, a plurality of reaction systems formula parallel with one another connects, and realizes continuous production.
7, the specific equipment of the processing method of the described continuous production glycerin fatty acid ester of a kind of claim 1, 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.
8, specific equipment according to claim 7 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, and the finished product delivery pipe that described intimate mixing pump discharge place is provided with is communicated with interchanger, and this interchanger is an one-level, this interchanger and lipid acid loading system or chilled(cooling) water supply (CWS) mechanism connection; Perhaps, this 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.
9, specific equipment according to claim 8, 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; Glycerine and catalyzer loading system contain temporary jar of storage tank, pump and catalyzer, be provided with heating tube in the described storage tank, this heating tube is communicated with heat-conducting oil furnace or steam boiler, steam or thermal oil are as pre-thermal medium, described storage tank is communicated with for temporary jar by described pump and described catalyzer, is provided with stirring mechanism in the temporary jar inner chamber of described catalyzer, and 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 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.
10, according to the arbitrary described specific equipment of claim 7-9, 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, 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.
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| JP3853552B2 (en) * | 1999-12-17 | 2006-12-06 | 花王株式会社 | Method for producing diglyceride |
| CN101070283A (en) * | 2006-05-08 | 2007-11-14 | 李普选 | Fatty-acid methyl ester producing process and apparatus |
| CN101225044B (en) * | 2008-02-01 | 2010-09-01 | 河南兴泰科技实业有限公司 | Methyl glycol fatty acid ester and preparation method thereof |
| CN201406393Y (en) * | 2009-04-29 | 2010-02-17 | 李普选 | Special device for continuously producing fatty glyceride |
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2009
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| 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 |
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| CN102276456A (en) * | 2011-06-20 | 2011-12-14 | 湖北东信药业有限公司 | Process for preparing pharmaceutical excipient mixed fatty acid glyceride |
| CN102276456B (en) * | 2011-06-20 | 2013-07-31 | 湖北东信药业有限公司 | Process for preparing pharmaceutical excipient mixed fatty acid glyceride |
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| CN105348104A (en) * | 2015-09-29 | 2016-02-24 | 浙江迪耳化工有限公司 | Production method of glycerin tribenzoate |
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