CN105017014A - Preparation method of neo-pentyl polyhydric alcohol heptanoic acid ester - Google Patents
Preparation method of neo-pentyl polyhydric alcohol heptanoic acid ester Download PDFInfo
- Publication number
- CN105017014A CN105017014A CN201510370888.2A CN201510370888A CN105017014A CN 105017014 A CN105017014 A CN 105017014A CN 201510370888 A CN201510370888 A CN 201510370888A CN 105017014 A CN105017014 A CN 105017014A
- Authority
- CN
- China
- Prior art keywords
- amyl
- based polyol
- acid
- lab scale
- enanthic acid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/08—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides with the hydroxy or O-metal group of organic compounds
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/48—Separation; Purification; Stabilisation; Use of additives
- C07C67/56—Separation; Purification; Stabilisation; Use of additives by solid-liquid treatment; by chemisorption
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a preparation method of a neo-pentyl polyhydric alcohol heptanoic acid ester. According to the preparation method, neo-pentyl polyhydric alcohol and heptylic acid are obtained via different batches; theoretical molar ratio required by complete esterification with heptylic acid is determined based on the number of hydroxy groups in neo-pentyl polyhydric alcohol or mixed neo-pentyl polyhydric alcohol molecules, or a plurality of pilot tests are carried out based on experience molar ratio of neo-pentyl polyhydric alcohol or mixed neo-pentyl polyhydric alcohol with heptylic acid; when the acid value of a pilot test sample is 1.5mgKOH/g or lower, and separation performance of a synthetic liquid with water is excellent, testing is stopped, and the raw material batch and the raw material ratio are used for large-scale production. The preparation method is capable of realizing full utilization of the raw materials, and avoiding troubles caused by product postprocessing.
Description
Technical field
The invention belongs to organic chemistry raw material and manufacture field, particularly a kind of preparation technology of amyl-based polyol heptanoate.
Background technology
In numerous fatty acid esters, a class fatty acid ester is had to have the special construction of quaternary carbon atom, also known as neopentyl structure, typical example as: pentaerythritol fatty ester, bis pentaervthritol ester, trimethylolpropane fatty acid ester, ditrimethylolpropane fatty acid ester, neopentyl glycol fatty acid ester, they enjoy the favor of people.Because the β position carbon atom of the carbonyl of these neo-pentyl fatty acid esters does not have hydrogen atom, so can not with the resonance structure of the carbon of the alcohol moiety of ester group and hydrogen evolution six atom cycloalkyl, only have high-energy could destroy such ester structure, this makes the stability of the oxidation-resistance of amyl-based polyol fatty acid ester and anti-elimination reaction fine.Thus amyl-based polyol fatty acid ester has the unrivaled superiority of other ester class, becomes the optimal selection of the high-end synthetic ester in current lubricating oil.
Not only thermal oxidation stability is good for amyl-based polyol fatty acid ester, heat decomposition temperature is high, and resistance to low temperature good, easily degrade in the environment, the lubricant in the synthetic base oil of lubricating oil and metal rolled process can be used as, so be more and more subject to people's attention.
Although enanthic acid is somewhat expensive, but it is as a kind of saturated fatty acid with odd numbers of carbon atoms number, synthesize with it and amyl-based polyol, high fatty alcohol etc. the synthetic ester obtained, obvious feature is exactly that the pour point of product is low, can use at low ambient temperatures.
The technique document of current synthesis amyl-based polyol fatty acid ester series products is many, nothing more than employing direct esterification and ester-interchange method.Ester-interchange method owing to using basic catalyst, and can produce lower aliphatic alcohols etc. and has inflammable and byproduct that is explosion hazard, so in fact use seldom.Even employing direct esterification, be mostly adopt the excessive reaction forward of impelling of certain raw material to carry out, this will run into excessive raw material and the difficulty of product separation in follow-up purification, treating process.Even if adopt the means such as molecule rectifying to remove certain excessive raw material, even if can take off very thorough, also will inevitably cause the decline of target product yield, and the energy consumption that sepn process brings thus also can not be ignored, be thus difficult to synthesize the competitive product of price.
The current production technique display of some document reflection, in the process of synthesis amyl-based polyol fatty acid ester, adopts solvent or water entrainer to improve the efficiency of dehydration, makes esterification be unlikely to just can carry out at relatively high temperatures thoroughly.But one that adopts such technique to bring fearful effect finally will allow these solvents or water entrainer and product realize being separated thoroughly also very difficult.And the existence of a small amount of low boiling point solvent or water entrainer can cause the flash-point of product obviously to decline, at high temperature use to product and bring hidden danger.
The also current production technique display of some document reflection, in order to improve esterification yield, reduce the time of reaction, often adopts the excessive way of lipid acid to react, then carries out aftertreatment to product.To in the aftertreatment of product, mostly adopt neutralization, washing and point equal purification means.The consequence adopting such technology to bring is that the raw material of these acidity has loss, unit consumption is difficult to reach desirable level, production cost remains high.The salt produced in N-process is difficult to removing, and the process that will meet environmental requirement to the salt be in waste water is also a thing that make repeated headache.Because used alkaline matter in the process of aftertreatment, there is the situation of saponification reaction in the ester that also may occur to be synthesized, product is gone wrong again in follow-up use procedure.
Double the disclosed process data about synthetic ester, can find in current Technology in the selection of catalyzer, mostly the catalyzer of abandoning tradition, use load miscellaneous or composite catalyst instead.The cost in fact preparing various novel catalyzer is just higher, and the catalytic effect of these novel catalyzer is good not as good as traditional catalyst.Even if some solid catalyst can reclaim, but along with the effective constituent of in use solid-carried catalyst is constantly by wash-out, in fact these catalyzer can reusable restricted lifetime.
Because the source of raw material is different, production technique is also not quite similar, the index such as purity, foreign matter content of different batches raw material also exists trickle fluctuation, so qualified amyl-based polyol fatty acid ester will be produced, also need the feature for different batches raw material to carry out lab scale to grope, the proportioning of Reasonable adjustment raw material.
For the quality fluctuation of raw material between the deficiency of existing production amyl-based polyol fatty acid ester Product Process and different batches, be necessary the harmony considered production control cost and take into account quality product, adopt the tosic acid be easy to get as catalyzer, in conjunction with determining rational proportioning between different batches raw material by lab scale, come economical, reasonably produce amyl-based polyol heptanoate.
Summary of the invention
The technical problem to be solved in the present invention is to provide and a kind of adopts tosic acid to be catalyzer, economic and preparation technology that is reasonably amyl-based polyol heptanoate.
For solving the problems of the technologies described above, technical scheme of the present invention is: a kind of preparation technology of amyl-based polyol heptanoate, and its innovative point is: for amyl-based polyol and the enanthic acid of purchasing the present lot come,
First determine the theoretical molar proportioning of carrying out with enanthic acid completely needed for esterification according to amyl-based polyol used or the quantity that mixes hydroxyl in new penta season polyol molecule, or according to former for amyl-based polyol or mix new penta season polyvalent alcohol and the experience mol ratio that formed of enanthic acid select the mol ratio of current lab scale;
Adopt tosic acid as catalyzer, rely on heating to carry out esterification when logical nitrogen, and the water taken out of with nitrogen is collected by collection device, observe in collection device and no longer included after water deviates from 5 ~ 20 minutes, sampling, the acid number of working sample, makes current lab scale sample meet acid number≤1.5mgKOH/g by the adjustment of one or many lab scale mol ratio;
Add adsorption decolouriser, continue heated and stirred 0.5 ~ 2h, then heating is stopped, when being cooled to 50 ~ 70 DEG C in lab scale sample, suction filtration is carried out while hot in the Büchner funnel being covered with middling speed quantitative paper, product in filter flask is transferred in reagent bottle, the method specified according to GB/T 7305-2003, measure the separation property of synthesis liquid and water; After if the result display high-speed stirring recorded terminates within three ten minutes left standstill after, the volume of emulsion layer is less than 3mL, then represent that the separation property of this synthesis liquid and water is good, terminate this lab scale;
Acid number≤1.5mgKOH/g in this lab scale and synthesis liquid and water separation property also satisfactory lab scale mol ratio carry out large-scale production as the proportioning raw materials of present lot raw material.
Further, described concrete steps are as follows:
step S1:for amyl-based polyol and the enanthic acid of purchasing the present lot come, the quantity calculating amyl-based polyol used or mix hydroxyl in new penta season polyol molecule determines the theoretical molar proportioning of carrying out with enanthic acid completely needed for esterification, according to former for amyl-based polyol or mix new penta season polyvalent alcohol and enanthic acid formed experience mol ratio carry out lab scale test, if the quantity of amounting to hydroxyl of the hydroxyl value of amyl-based polyol used or mixing amyl-based polyol is n, then enanthic acid and amyl-based polyol or mix amyl-based polyol theoretical molar than being n,
step S2:the mol ratio setting amyl-based polyol and enanthic acid in this lab scale is 0.9:n ~ 1.2:n;
step S3:carry out lab scale, in the three-necked bottle of 500mL, first put into magnetic stir bar, drop into the enanthic acid of 0.4 ~ 1.2mol, then according to the mol ratio that sets in step S2 drop into respective amount amyl-based polyol or mix new penta season polyvalent alcohol, open the intensification switch of oil bath heater, material in still is heated, when temperature in the kettle is raised to 110 ± 4 DEG C, add enanthic acid and amyl-based polyol used or mix new penta season polyvalent alcohol always feed intake quality 0.5 ~ 2% tosic acid as catalyzer, under nitrogen tube is inserted into liquid level, nitrogen is passed into the flow velocity of 10 ~ 100mL/min, open the stirring of stirrer in magnetic agitation still, timing from now, material in still is warmed up to 120 ~ 250 DEG C, heating 5 ~ 24h, the water of observing response by-product is deviate to the speed conditions in collection device under the drive of nitrogen, by the time no longer included after a water deviates from collection device in 5 ~ 20 minutes, sampling,
step S4:the acid number of working sample, if the acid number≤1.5mgKOH/g of sample, then leaps to step S9; If the acid number > 1.5mgKOH/g of sample, then enter next step;
step S5:continue reaction 0.5 ~ 2h;
step S6:the reacted acid number of sampling and measuring, if acid number≤1.5mgKOH/g, then jumps to step S9; If acid number > is 1.5mgKOH/g, then enter next step;
step S7:judge the absolute value of acid number and the adjacent last hypo acid value difference measured in above-mentioned steps S6, if this absolute value > is 0.5mgKOH/g, then return step S5; If this absolute value≤0.5mgKOH/g, then enter next step;
step S8:if acid number is > 1.5mgKOH/g still, then terminate this lab scale, and return step S2 and again adjust in the scope of 0.9:n ~ 1.2:n and set once the concrete mol ratio that amyl-based polyol and enanthic acid lab scale test; If acid number≤1.5mgKOH/g, then enter next step;
step S9:in three-necked bottle, add amyl-based polyol used or mix new penta season polyvalent alcohol and enanthic acid always feed intake quality 0.5 ~ 5%, particle diameter is the adsorption decolouriser of 65 ~ 80 μm, continue heated and stirred 0.5 ~ 2h, then heating is stopped, when being cooled to 50 ~ 70 DEG C in lab scale sample, in the Büchner funnel being covered with middling speed quantitative paper, carry out suction filtration while hot, the product in filter flask is transferred in reagent bottle;
step S10:according to the method that GB/T 7305-2003 specifies, synthesis liquid in mensuration reagent bottle and the separation property of water, if be less than 3mL at the volume of the three ten minutes internal emulsification layers left standstill after the result display high-speed stirring recorded terminates, then represent that the separation property of this synthesis liquid and water is good, terminate this lab scale, write down this batch of enanthic acid used and the suitable mol ratio of amyl-based polyol, using the mol ratio of this lab scale as proportioning raw materials when carrying out large-scale production with the raw material of present lot; If measurement result display synthesis liquid and the separation property of water bad, then return step S2, in the test of fine setting lab scale enanthic acid and amyl-based polyol or mix new penta season polyvalent alcohol concrete mol ratio, then carry out lab scale next time;
step S11:large-scale production;
Further, the step of described large-scale production is specially:
step S111:the present lot obtained with lab scale amyl-based polyol used or mix new penta season polyvalent alcohol and the mol ratio of enanthic acid, at 2M
3reactor in, drop into enanthic acid and amyl-based polyol or mix new penta season polyvalent alcohol, the total mass of raw material in still is made to be in the scope of 500 ~ 1500kg, open and stir, during beginning, rotating speed maintains 5 ~ 50rpm, open the heating valve of reactor, material in still is heated, when temperature in the kettle is raised to 115 ± 5 DEG C, add enanthic acid and amyl-based polyol used or mix new penta season polyvalent alcohol always feed intake quality 0.5 ~ 2% tosic acid as catalyzer, open nitrogen valve, nitrogen is passed into the flow velocity of 1 ~ 100L/min, the rotating speed of stirring is brought up to 50 ~ 300rpm, timing from now, material in still is warmed up to 120 ~ 250 DEG C, heating 5 ~ 24h, the water of observing response by-product is deviate to the speed conditions in collection device under the drive of nitrogen, by the time no longer included after a water deviates from collection device in 5 ~ 20 minutes, sampling, the acid number of working sample,
step S112:if the acid number of sample can not reach≤level of 1.5mgKOH/g, then carry out reaction 0.5 ~ 2h, resampling detects acid number, until the acid number≤1.5mgKOH/g of sample;
step S113:in reactor, add amyl-based polyol used or mix new penta season polyvalent alcohol and enanthic acid always feed intake quality 0.1 ~ 2% adsorption decolouriser, continue heated and stirred 0.5 ~ 3h, then heating is stopped, when being cooled to 50 ~ 70 DEG C Deng the temperature of product in still, open the valve at the bottom of still, with refining filtering pump by flow out material pumping in pressure filter, order number is adopted to be 250 ~ 300 object filter screens, carry out circulation press filtration, press filtration material out turns back in reactor, the color that circulation press filtration proceeds to the product returned do not seen adsorption decolouriser particle residual till, product after press filtration being decoloured pours in pail pack.
Further, described amyl-based polyol or mix new penta season polyvalent alcohol be one or more in TriMethylolPropane(TMP), ditrimethylolpropane, tetramethylolmethane, dipentaerythritol, neopentyl glycol.
Further, described adsorption decolouriser can be gac, atlapulgite, attapulgite, diatomite.
Further, described adsorption decolouriser can be gac, atlapulgite, attapulgite, diatomite.
The invention has the advantages that:
(1) each batch of raw material owing to buying has trickle fluctuation in purity, so adopt in the theoretical molar proportioning of corresponding raw material or the basis of experience mol ratio, the raw material of each batch is first adjusted to their proportioning by lab scale, until the acid number of amyl-based polyol fatty acid ester that lab scale is synthesized both met the requirements, also after meeting the requirements with the separation property of water, the feed molar proportioning adopting this suitable again goes to carry out large-scale production, raw material can be made to be fully utilized, ensure the quality of product, eliminate the highly energy-consuming that molecule rectifying is such, the lossy post-processing step of product, make production process economy, rationally, product has the market competitiveness.
(2) need not as current some processes, high, the not poisonous organic solvent of the boiling point such as toluene, dimethylbenzene is adopted to go as water entrainer, avoid the Dangerous and Harmful Factors in operating process, there is not the residual of low-boiling-point substance in product, thus ensure that the amyl-based polyol fatty acid ester be synthesized can at high temperature use.
(3) lipid acid owing to not adopting some traditional technologys to adopt is excessive, and then the technique that neutralizes is carried out with alkaline solution, eliminate washing and point equal post-processing step, and reluctant salts substances can not be produced, make that production process seems succinctly, environmental protection, avoid the product that is synthesized in the basic conditions again by the risk of saponification, hydrolysis.
(4) adopt traditional tosic acid as catalyzer, conveniently be easy to get, not exist batch between the discrepant problem of catalytic activity, it also has a benefit, be exactly that its fusing point is about 106 DEG C, after reaction end product cools down, in the process of decolorization filtering, the tosic acid of separating out from system can be filtered out together, realize being separated of catalyzer and product.
(5) when adopting gac as adsorption decolouriser, when gac price is higher, be combined the porousness sorbent material that diatomite, attapulgite, atlapulgite etc. are inexpensive, can the rational thickness of filter bed of heap, both be enough to play good filtration decolorizing effect in suction filtration or circulation pressure-filtering process, and effectively can have reduced again the cost of decolorization.
Embodiment
The following examples can make the present invention of professional and technical personnel's comprehend, but therefore do not limit the present invention among described scope of embodiments.
embodiment 1
A preparation method for amyl-based polyol heptanoate, adopt TriMethylolPropane(TMP) and enanthic acid to be raw material, concrete steps comprise:
step S1:the TriMethylolPropane(TMP) of present lot that buying is come and enanthic acid, the quantity of the hydroxyl contained due to a part TriMethylolPropane(TMP) is 3, then enanthic acid is 3 with the theoretical molar ratio of TriMethylolPropane(TMP);
step S2:set the mol ratio of enanthic acid and TriMethylolPropane(TMP) in this lab scale, synthesize according to front the experience drawn several times, TriMethylolPropane(TMP) and the proper mol ratio of enanthic acid are 1.05:3;
step S3:carry out lab scale, in the three-necked bottle of 500mL, first put into magnetic stir bar, drop into 1.2mol(156.216g) enanthic acid, then correspondingly drop into 0.42mol(56.351g) TriMethylolPropane(TMP), open the intensification switch of oil bath heater, material in still is heated, when temperature in the kettle is raised to 110 DEG C, add enanthic acid and TriMethylolPropane(TMP) always to feed intake the 1%(2.13g of quality 212.567g) tosic acid as catalyzer, under nitrogen tube is inserted into liquid level, nitrogen is passed into the flow velocity of 30mL/min, open the stirring of stirrer in magnetic agitation still, timing from now, material in still is warmed up to 180 ± 5 DEG C, heating 10h, the water of observing response by-product is deviate to the speed conditions in collection device under the drive of nitrogen, by the time no longer included after a water deviates from collection device in 10 minutes, sampling,
step S4:the acid number of working sample is 0.58mgKOH/g, due to the acid number≤1.5mgKOH/g of sample, then leaps to step S9;
step S9:in three-necked bottle, adding TriMethylolPropane(TMP) and enanthic acid always to feed intake the 2%(4.25g of quality) particle diameter is the atlapulgite of 75 μm, continue heated and stirred 1h, then heating is stopped, when being cooled to 60 DEG C in lab scale sample, in the Büchner funnel being covered with middling speed quantitative paper, carry out suction filtration while hot, the product in filter flask is transferred in reagent bottle;
step S10:according to the method that GB/T 7305-2003 specifies, measure the separation property of synthesis liquid and water, the result recorded be high-speed stirring terminate rear leave standstill ten minutes time, between oil phase and aqueous phase, the volume of emulsion layer is 1mL, represent that the separation property of this synthesis liquid and water is good, so need not adjust the mol ratio of this batch of TriMethylolPropane(TMP) relative to enanthic acid again; Terminate this lab scale, write down this batch of enanthic acid used and the suitable mol ratio of TriMethylolPropane(TMP), using the mol ratio of this lab scale as proportioning raw materials when carrying out large-scale production with the raw material of present lot;
step S11:large-scale production;
Be specially:
Step S111: the suitable mol ratio 1.05:3 adopting the TriMethylolPropane(TMP) for present lot and the enanthic acid obtained in above-mentioned steps, at 2M
3reactor in, drop into 781.08kg enanthic acid and 281.757kg TriMethylolPropane(TMP), the total mass of raw material in still is made to reach 1062.837kg, open and stir, during beginning, rotating speed maintains 15rpm, open the heating valve of reactor, material in still is heated, when temperature in the kettle is raised to 115 DEG C, add enanthic acid and TriMethylolPropane(TMP) always to feed intake the 1.0%(10.63kg of quality) tosic acid as catalyzer, open nitrogen valve, nitrogen is passed into the flow velocity of 20L/min, the rotating speed of stirring is brought up to 150rpm, timing from now, material in still is warmed up to 180 ± 5 DEG C, heating 10.5h, the water of observing response by-product is deviate to the speed conditions in collection device under the drive of nitrogen, by the time no longer included after a water deviates from collection device in 10 minutes, sampling, the acid number of working sample, for 0.62mgKOH/g,
Step S112: because the acid number of sample reaches≤the level of 1.5mgKOH/g, so need not proceed reaction again;
Step S113: add TriMethylolPropane(TMP) and enanthic acid and always feed intake the 0.5%(5.31kg of quality in reactor) particle diameter is the atlapulgite of 75 μm, continue heated and stirred 2h, then heating is stopped, when being cooled to 60 DEG C Deng the temperature of product in still, open the valve at the bottom of still, with refining filtering pump by flow out material pumping in pressure filter, employing order number is that the filter screen of 270 μm carries out circulation press filtration, press filtration material out turns back in reactor, after circulation press filtration carries out six minutes, the color of the product returned has not seen the residual of atlapulgite particle, product after press filtration being decoloured pours in pail pack.
embodiment 2
Produce a method for ditrimethylolpropane heptanoate, adopt ditrimethylolpropane and enanthic acid to be raw material, concrete steps comprise:
step S1:for ditrimethylolpropane and the enanthic acid of purchasing the present lot come, have 4 hydroxyls in a ditrimethylolpropane molecule, then enanthic acid is 4 with the theoretical molar ratio of ditrimethylolpropane;
step S2:set the mol ratio of enanthic acid and ditrimethylolpropane in this lab scale, combine according to the front experience drawn of synthesizing several times with theoretical molar ratio, ditrimethylolpropane and the proper mol ratio of enanthic acid are 1.05:4;
step S3:carry out lab scale, in the three-necked bottle of 500mL, first put into magnetic stir bar, drop into 1.2mol(156.216g) enanthic acid, then correspondingly drop into 0.315mol(78.854g) ditrimethylolpropane, open the intensification switch of oil bath heater, material in still is heated, when temperature in the kettle is raised to 110 DEG C, add enanthic acid and ditrimethylolpropane always to feed intake the 1%(2.35g of quality 235.07g) tosic acid as catalyzer, under nitrogen tube is inserted into liquid level, nitrogen is passed into the flow velocity of 30mL/min, open the stirring of stirrer in magnetic agitation still, timing from now, material in still is warmed up to 160 ± 5 DEG C, heating 6.5h, the water of observing response by-product is deviate to the speed conditions in collection device under the drive of nitrogen, by the time no longer included after a water deviates from collection device in 10 minutes, sampling,
step S4:the acid number of working sample is 0.8mgKOH/g, because the acid number of sample reaches≤the level of 1.5mgKOH/g, leaps to step S9 so subsequent;
step S9:in three-necked bottle, adding ditrimethylolpropane and enanthic acid always to feed intake the 1%(2.35g of quality) particle diameter is the gac of 75 μm, continue heated and stirred 1h, then heating is stopped, when being cooled to 60 DEG C in lab scale sample, be carry out suction filtration in the Büchner funnel of the diatomite of 75 μm and middling speed quantitative paper being covered with particle diameter while hot, the product in filter flask is transferred in reagent bottle;
step S10:according to the method that GB/T 7305-2003 specifies, measure the separation property of synthesis liquid and water, the result recorded is that when leaving standstill 30 minutes after high-speed stirring terminates, between oil phase and aqueous phase, the volume of emulsion layer is 5mL, represents that the separation property of this synthesis liquid and water is bad, the separation property of synthesizing liquid and water due to the result display recorded is bad, so return step S2, adjusting this batch of ditrimethylolpropane relative to the mol ratio of enanthic acid is 1.03:4, drop into 1.2mol(156.216g) enanthic acid, then correspondingly drop into 0.309mol(77.352g) ditrimethylolpropane, the rapid S3 of all the other course synchronization of lab scale synthesis, then decolour, filter, measure the separation property of synthesis liquid and water, the result recorded is that high-speed stirring terminates rear leaving standstill after 20 minutes, between oil phase and aqueous phase, the volume of emulsion layer is 2mL, represent that the separation property of this synthesis liquid and water can accept, write down this batch of ditrimethylolpropane used and the suitable mol ratio 1.03:4 of enanthic acid,
step S11:large-scale production;
Be specially:
Step S111: the suitable mol ratio 1.03:4 adopting the ditrimethylolpropane for present lot and the enanthic acid obtained in above-mentioned steps, at 2M
3reactor in, drop into 781.08kg enanthic acid and 387.76kg ditrimethylolpropane, the total mass of raw material in still is made to reach 1167.84kg, open and stir, during beginning, rotating speed maintains 15rpm, open the heating valve of reactor, material in still is heated, when temperature in the kettle is raised to 115 DEG C, add enanthic acid and ditrimethylolpropane always to feed intake the 0.8%(9.34kg of quality) tosic acid as catalyzer, open nitrogen valve, nitrogen is passed into the flow velocity of 20L/min, the rotating speed of stirring is brought up to 150rpm, timing from now, material in still is warmed up to 160 ± 5 DEG C, heating 7h, the water of observing response by-product is deviate to the speed conditions in collection device under the drive of nitrogen, by the time no longer included after a water deviates from collection device in 10 minutes, sampling, the acid number of working sample, for 1.2mgKOH/g,
Step S112: because the acid number of sample reaches≤the level of 1.5mgKOH/g, so need not proceed reaction again;
Step S113: add ditrimethylolpropane and enanthic acid and always feed intake the 0.3%(3.5kg of quality in reactor) particle diameter is the gac of 75 μm, 0.15%(1.75kg) particle diameter is the diatomite of 75 μm, continue heated and stirred 1.5h, then heating is stopped, when being cooled to 60 DEG C Deng the temperature of product in still, open the valve at the bottom of still, with refining filtering pump by flow out material pumping in pressure filter, order number is adopted to be 270 object filter screens, carry out circulation press filtration, press filtration material out turns back in reactor, after circulation press filtration carries out four minutes, the color of the product returned has not seen that the activated carbon granule of diatomite particle and black remains, product after press filtration being decoloured pours in pail pack.
embodiment 3
A preparation method for amyl-based polyol heptanoate, adopt tetramethylolmethane and enanthic acid to be raw material, concrete steps are as follows:
step S1:for tetramethylolmethane and the enanthic acid of purchasing the present lot come, have 4 hydroxyls in a tetramethylolmethane molecule, then enanthic acid is 4 with the theoretical molar ratio of tetramethylolmethane;
step S2:set the mol ratio of enanthic acid and tetramethylolmethane in this lab scale, the theoretical molar proportioning 1:4 both first adopting;
step S3:carry out lab scale, in the three-necked bottle of 500mL, first put into magnetic stir bar, drop into 1.2mol(156.216g) enanthic acid, then correspondingly drop into 0.3mol(40.845g) tetramethylolmethane, open the intensification switch of oil bath heater, material in still is heated, when temperature in the kettle is raised to 110 DEG C, add enanthic acid and tetramethylolmethane always to feed intake the 1%(1.97g of quality 197.061g) tosic acid as catalyzer, under nitrogen tube is inserted into liquid level, nitrogen is passed into the flow velocity of 30mL/min, open the stirring of stirrer in magnetic agitation still, timing from now, material in still is warmed up to 190 ± 5 DEG C, heating 15h, the water of observing response by-product is deviate to the speed conditions in collection device under the drive of nitrogen, by the time no longer included after a water deviates from collection device in 10 minutes, sampling,
step S4:the acid number of working sample is 2.8mgKOH/g, because the acid number of sample does not reach≤the level of 1.5mgKOH/g, enters next step;
step S5:continue reaction 1h;
step S6:the reacted acid number of sampling and measuring is 2.5mgKOH/g, due to acid number > 1.5mgKOH/g, enters next step;
step S7:judge the absolute value of acid number and the adjacent last hypo acid value difference measured in above-mentioned steps S6, due to this absolute value≤0.5mgKOH/g, enter next step;
step S8:due to current acid number still > 1.5mgKOH/g, terminate this lab scale, and return step S2, again adjusting in the scope of 0.9:n ~ 1.2:n and setting once the concrete mol ratio that tetramethylolmethane and enanthic acid lab scale test is 1.05:4, drop into 1.2mol(156.216g) enanthic acid, then correspondingly drop into 0.315mol(42.887g) tetramethylolmethane, all the other process repeats step S3, reaction 15h, sampling, the sample acid number recorded is 0.8mgKOH/g, has reached the requirement of acid number≤1.5mgKOH/g, has entered next step;
step S9:in three-necked bottle, adding tetramethylolmethane and enanthic acid always to feed intake the 1%(1.97g of quality) particle diameter is the gac of 75 μm, continue heated and stirred 1h, then heating is stopped, when being cooled to 60 DEG C in lab scale sample, be carry out suction filtration in the Büchner funnel of the attapulgite of 75 μm and middling speed quantitative paper being covered with particle diameter while hot, the product in filter flask is transferred in reagent bottle;
step S10:according to the method that GB/T 7305-2003 specifies, measure the separation property of synthesis liquid and water, the result recorded is when leaving standstill 20 minutes after high-speed stirring terminates, between oil phase and aqueous phase, the volume of emulsion layer is 0mL, represent that the separation property of this synthesis liquid and water is fine, terminate this lab scale, write down this batch of tetramethylolmethane and the suitable mol ratio of enanthic acid, for 1.05:4, using the proportioning raw materials of this lab scale as proportioning raw materials when carrying out large-scale production with the raw material of present lot;
step S11:large-scale production;
Be specially:
Step S111: the suitable mol ratio 1.05:4 adopting the tetramethylolmethane for present lot and the enanthic acid obtained in above-mentioned steps, at 2M
3reactor in, drop into 781.08kg enanthic acid and 214.436kg tetramethylolmethane, the total mass of raw material in still is made to reach 995.516kg, open and stir, during beginning, rotating speed maintains 15rpm, open the heating valve of reactor, material in still is heated, when temperature in the kettle is raised to 115 DEG C, add enanthic acid and tetramethylolmethane always to feed intake the 1%(9.96kg of quality) tosic acid as catalyzer, open nitrogen valve, nitrogen is passed into the flow velocity of 50L/min, the rotating speed of stirring is brought up to 150rpm, timing from now, material in still is warmed up to 190 ± 5 DEG C, heating 16h, the water of observing response by-product is deviate to the speed conditions in collection device under the drive of nitrogen, by the time no longer included after a water deviates from collection device in 10 minutes, sampling, the acid number of working sample, for 0.86mgKOH/g,
Step S112: because the acid number of sample reaches≤the level of 1.5mgKOH/g, so need not proceed reaction again;
Step S113: add tetramethylolmethane and enanthic acid and always feed intake the 0.4%(3.98kg of quality in reactor) particle diameter is the gac of 75 μm, 0.2%(1.99kg) particle diameter is the attapulgite of 75 μm, continue heated and stirred 1.5h, then heating is stopped, when being cooled to 60 DEG C Deng the temperature of product in still, open the valve at the bottom of still, with refining filtering pump by flow out material pumping in pressure filter, order number is adopted to be 270 object filter screens, carry out circulation press filtration, press filtration material out turns back in reactor, after circulation press filtration carries out eight minutes, the color of the product returned has not seen that the attapulgite particle of brown and the activated carbon granule of black remain, product after press filtration being decoloured pours in pail pack.
embodiment 4
A preparation method for amyl-based polyol heptanoate, the mixing amyl-based polyol that employing mass percent accounts for the tetramethylolmethane of 90%, the dipentaerythritol of 10% forms and enanthic acid are raw material, and concrete steps are as follows:
step S1:4 hydroxyls are had in a tetramethylolmethane molecule, 6 hydroxyls are had in a dipentaerythritol molecule, account for the tetramethylolmethane of 90% by mass percent, the molecular-weight average of mixing amyl-based polyol that the dipentaerythritol of 10% forms is 142.783, amounting to hydroxyl value is 4.112, for this mixing amyl-based polyol that the tetramethylolmethane come with buying and dipentaerythritol are mixed with, be 1:4.112 relative to the theoretical molar proportioning of enanthic acid;
step S2:set the mol ratio of enanthic acid and amyl-based polyol in this lab scale, this lab scale directly adopts theoretical molar proportioning 1:4.112;
step S3:carry out lab scale, in the three-necked bottle of 500mL, first put into magnetic stir bar, drop into 1.234mol(160.602g) enanthic acid, then correspondingly drop into 0.3mol(42.835g) mixing amyl-based polyol, open the intensification switch of oil bath heater, material in still is heated, when temperature in the kettle is raised to 110 DEG C, add enanthic acid and mixing amyl-based polyol always to feed intake the 1%(2.03g of quality 203.437g) tosic acid as catalyzer, under nitrogen tube is inserted into liquid level, nitrogen is passed into the flow velocity of 30mL/min, open the stirring of stirrer in magnetic agitation still, timing from now, material in still is warmed up to 240 ± 5 DEG C, heating 18h, the water of observing response by-product is deviate to the speed conditions in collection device under the drive of nitrogen, by the time no longer included after a water deviates from collection device in 10 minutes, sampling,
step S4:the acid number of working sample is 0.2mgKOH/g, because the acid number of sample reaches≤the level of 1.5mgKOH/g, leaps to the S9 of conventional steps so subsequent;
step S9:in three-necked bottle, adding mixing amyl-based polyol and enanthic acid always to feed intake the 1%(2.03g of quality) particle diameter is the attapulgite of 75 μm, continue heated and stirred 1.5h, then heating is stopped, when being cooled to 60 DEG C in lab scale sample, in the Büchner funnel being covered with middling speed quantitative paper, carry out suction filtration while hot, the product in filter flask is transferred in reagent bottle;
step S10:according to the method that GB/T 7305-2003 specifies, measure the separation property of synthesis liquid and water, the result recorded is that high-speed stirring terminates rear leaving standstill after 30 minutes, and between oil phase and aqueous phase, the volume of emulsion layer is 5mL, represents that the separation property of this synthesis liquid and water is bad;
Need to return step S2, finely tuning enanthic acid in lab scale test is next time 0.97:4.112 with this concrete mol ratio mixing amyl-based polyol, drop into 1.234mol(160.602g) enanthic acid, then correspondingly drop into 0.291mol(41.550g) mixing amyl-based polyol, the rapid S3 of all the other course synchronization of lab scale synthesis, to the product sampling synthesized, recording its acid number is 0.6mgKOH/g, meet the requirements, proceed decolouring, filter, and then measure the separation property of synthesis liquid and water, the result recorded is that high-speed stirring terminates rear leaving standstill after 20 minutes, between oil phase and aqueous phase, the volume of emulsion layer is 2mL, represent that the separation property of this synthesis liquid and water can accept, writing down for the mixing amyl-based polyol of this batch of preparation and the suitable mol ratio of enanthic acid raw material is 0.97:4.112, using the proportioning raw materials of this lab scale as proportioning raw materials when carrying out large-scale production with the raw material of present lot,
step S11:large-scale production;
Be specially:
Step S111: adopt in above-mentioned steps obtain for the mixing amyl-based polyol of present lot and the suitable mol ratio 0.97:4.112 of enanthic acid, at 2M
3reactor in, drop into the mixing amyl-based polyol of 781.08kg enanthic acid and 202.076kg preparation, the total mass of raw material in still is made to reach 983.156kg, open and stir, during beginning, rotating speed maintains 15rpm, open the heating valve of reactor, material in still is heated, when temperature in the kettle is raised to 115 DEG C, add enanthic acid and mixing amyl-based polyol always to feed intake the 1%(9.83kg of quality) tosic acid as catalyzer, open nitrogen valve, nitrogen is passed into the flow velocity of 20L/min, the rotating speed of stirring is brought up to 150rpm, timing from now, material in still is warmed up to 240 ± 5 DEG C, heating 19h, the water of observing response by-product is deviate to the speed conditions in collection device under the drive of nitrogen, by the time no longer included after a water deviates from collection device in 10 minutes, sampling, the acid number of working sample, for 0.66mgKOH/g,
Step S112: because the acid number of sample reaches≤the level of 1.5mgKOH/g, so need not proceed reaction again;
Step S113: add the mixing amyl-based polyol of preparation and enanthic acid and always feed intake the 0.6%(5.90kg of quality in reactor) particle diameter is the attapulgite of 75 μm, continue heated and stirred 2h, then heating is stopped, when being cooled to 60 DEG C Deng the temperature of product in still, open the valve at the bottom of still, with refining filtering pump by flow out material pumping in pressure filter, employing order number is that the filter screen of 270 μm carries out circulation press filtration, press filtration material out turns back in reactor, after circulation press filtration carries out ten minutes, the color of the product returned has not seen the residual of the attapulgite particle of brown, product after press filtration being decoloured pours in pail pack.
embodiment 5
A preparation method for amyl-based polyol heptanoate, adopt neopentyl glycol and enanthic acid to be raw material, concrete steps are as follows:
step S1:for neopentyl glycol and the enanthic acid of purchasing the present lot come, have 2 hydroxyls in a neopentyl glycol molecule, then the theoretical molar of enanthic acid and neopentyl glycol is than being 2:1;
step S2:set the mol ratio of enanthic acid and neopentyl glycol in this lab scale, synthesize according to front the experience drawn several times, neopentyl glycol and the proper mol ratio of enanthic acid are 1.02:2;
step S3:in the three-necked bottle of 500mL, first put into magnetic stir bar, drop into 1.6mol(208.288g) enanthic acid, then correspondingly drop into 0.816mol(84.896g) neopentyl glycol, open the intensification switch of oil bath heater, material in still is heated, when temperature in the kettle is raised to 110 DEG C, add enanthic acid and neopentyl glycol always to feed intake the 1%(2.93g of quality 293.274g) tosic acid as catalyzer, under nitrogen tube is inserted into liquid level, nitrogen is passed into the flow velocity of 30mL/min, open the stirring of stirrer in magnetic agitation still, timing from now, material in still is warmed up to 140 ± 5 DEG C, heating 5h, the water of observing response by-product is deviate to the speed conditions in collection device under the drive of nitrogen, by the time no longer included after a water deviates from collection device in 10 minutes, sampling,
step S4:the acid number of working sample is 2.5mgKOH/g, because the acid number of sample does not reach≤the level of 1.5mgKOH/g, therefore enters next step;
step S5:continue reaction 1h;
step S6:the reacted acid number of sampling and measuring, it is 1.6mgKOH/g that sampling detects acid number; Because its acid number does not still reach≤the level of 1.5mgKOH/g, therefore continue to enter step S7;
step S7:judge the absolute value of acid number and the adjacent last hypo acid value difference measured in above-mentioned steps S6, due to this absolute value > 0.5mgKOH/g, return step S5, continue reaction 1h, and then sample, the acid number of working sample, be 1.2 mgKOH/g, enter next step;
step S8:due to third time, the acid number of sample reaches≤the level of 1.5mgKOH/g, subsequently enters step S9;
step S9:in three-necked bottle, add neopentyl glycol and enanthic acid always to feed intake the 2%(5.865g of quality) particle diameter be the diatomite of 75 μm, continue heated and stirred 1h, then heating is stopped, when being cooled to 60 DEG C in lab scale sample, in the Büchner funnel being covered with middling speed quantitative paper, carry out suction filtration while hot, the product in filter flask is transferred in reagent bottle;
step S10:according to the method that GB/T 7305-2003 specifies, measure the separation property of synthesis liquid and water, the result recorded be high-speed stirring terminate rear leave standstill ten minutes time, between oil phase and aqueous phase, the volume of emulsion layer is 2mL, represent that the separation property of this synthesis liquid and water is good, writing down this batch of neopentyl glycol and the suitable mol ratio of enanthic acid, is 1.02:2, using the proportioning raw materials of this lab scale as proportioning raw materials when carrying out large-scale production with the raw material of present lot;
step S11:large-scale production;
Be specially:
Step S111: the suitable mol ratio 1.02:2 adopting the neopentyl glycol for present lot and the enanthic acid obtained in above-mentioned steps, at 2M
3reactor in, drop into 781.08kg enanthic acid and 318.699kg neopentyl glycol, the total mass of raw material in still is made to reach 1099.779kg, open and stir, during beginning, rotating speed maintains 20rpm, open the heating valve of reactor, material in still is heated, when temperature in the kettle is raised to 115 DEG C, add enanthic acid and neopentyl glycol always to feed intake the 1.0%(10.998kg of quality) tosic acid as catalyzer, open nitrogen valve, nitrogen is passed into the flow velocity of 20L/min, the rotating speed of stirring is brought up to 180rpm, timing from now, material in still is warmed up to 140 ± 5 DEG C, heating 7.5h, the water of observing response by-product is deviate to the speed conditions in collection device under the drive of nitrogen, by the time no longer included after a water deviates from collection device in 10 minutes, sampling, the acid number of working sample, for 1.3mgKOH/g,
Step S112: because the acid number of sample reaches≤the level of 1.5mgKOH/g, so need not proceed reaction again;
Step S113: add neopentyl glycol and enanthic acid and always feed intake the 0.6%(6.60kg of quality in reactor) particle diameter is the diatomite of 75 μm, continue heated and stirred 2h, then heating is stopped, when being cooled to 60 DEG C Deng the temperature of product in still, open the valve at the bottom of still, with refining filtering pump by flow out material pumping in pressure filter, employing order number is that the filter screen of 270 μm carries out circulation press filtration, press filtration material out turns back in reactor, after circulation press filtration carries out three minutes, the color of the product returned has not seen the residual of diatomite particle, product after press filtration being decoloured pours in pail pack.
Above content shows and describes ultimate principle of the present invention and principal character.The technician of the industry should understand; the present invention is not restricted to the described embodiments; what describe in above-described embodiment and specification sheets just illustrates principle of the present invention; without departing from the spirit and scope of the present invention; the present invention also has various changes and modifications, and these changes and improvements all fall in the claimed scope of the invention.Application claims protection domain is defined by appending claims and equivalent thereof.
Claims (8)
1.
a kind ofthe preparation technology of amyl-based polyol heptanoate, is characterized in that: described preparation technology is amyl-based polyol and enanthic acid for purchasing the present lot come; First determine the theoretical molar proportioning of carrying out with enanthic acid completely needed for esterification according to amyl-based polyol used or the quantity that mixes hydroxyl in new penta season polyol molecule, or according to former for amyl-based polyol or mix new penta season polyvalent alcohol and the experience mol ratio that formed of enanthic acid select the mol ratio of current lab scale; Adopt tosic acid as catalyzer, rely on heating to carry out esterification when logical nitrogen, and the water taken out of with nitrogen is collected by collection device, observe in collection device and no longer included after water deviates from 5 ~ 20 minutes, sampling, the acid number of working sample, makes current lab scale sample meet acid number≤1.5mgKOH/g by the adjustment of one or many lab scale mol ratio; Add adsorption decolouriser, continue heated and stirred 0.5 ~ 2h, then heating is stopped, when being cooled to 50 ~ 70 DEG C in lab scale sample, suction filtration is carried out while hot in the Büchner funnel being covered with middling speed quantitative paper, product in filter flask is transferred in reagent bottle, the method specified according to GB/T 7305-2003, measure the separation property of synthesis liquid and water; After if the result display high-speed stirring recorded terminates within three ten minutes left standstill after, the volume of emulsion layer is less than 3mL, then represent that the separation property of this synthesis liquid and water is good, terminate this lab scale; Acid number≤1.5mgKOH/g in this lab scale and synthesis liquid and water separation property also satisfactory lab scale mol ratio carry out large-scale production as the proportioning raw materials of present lot raw material.
2. the preparation technology of amyl-based polyol heptanoate according to claim 1, is characterized in that described concrete steps are as follows:
step S1:for amyl-based polyol and the enanthic acid of purchasing the present lot come, the quantity calculating amyl-based polyol used or mix hydroxyl in new penta season polyol molecule determines the theoretical molar proportioning of carrying out with enanthic acid completely needed for esterification, according to former for amyl-based polyol or mix new penta season polyvalent alcohol and enanthic acid formed experience mol ratio carry out lab scale test, if the quantity of amounting to hydroxyl of the hydroxyl value of amyl-based polyol used or mixing amyl-based polyol is n, then enanthic acid and amyl-based polyol or mix amyl-based polyol theoretical molar than being n,
step S2:the mol ratio setting amyl-based polyol and enanthic acid in this lab scale is 0.9:n ~ 1.2:n,
step S3:carry out lab scale, in the three-necked bottle of 500mL, first put into magnetic stir bar, drop into the enanthic acid of 0.4 ~ 1.2mol, then according to the mol ratio that sets in step S2 drop into respective amount amyl-based polyol or mix new penta season polyvalent alcohol, open the intensification switch of oil bath heater, material in still is heated, when temperature in the kettle is raised to 110 ± 4 DEG C, add enanthic acid and amyl-based polyol used or mix new penta season polyvalent alcohol always feed intake quality 0.5 ~ 2% tosic acid as catalyzer, under nitrogen tube is inserted into liquid level, nitrogen is passed into the flow velocity of 10 ~ 100mL/min, open the stirring of stirrer in magnetic agitation still, timing from now, material in still is warmed up to 120 ~ 250 DEG C, heating 5 ~ 24h, the water of observing response by-product is deviate to the speed conditions in collection device under the drive of nitrogen, by the time no longer included after a water deviates from collection device in 5 ~ 20 minutes, sampling,
step S4:the acid number of working sample, if the acid number≤1.5mgKOH/g of sample, then leaps to step S9, if the acid number > 1.5mgKOH/g of sample, then enter next step,
step S5:continue reaction 0.5 ~ 2h;
step S6:the reacted acid number of sampling and measuring, if acid number≤1.5mgKOH/g, then jumps to step S9; If acid number > is 1.5mgKOH/g, then enter next step;
step S7:judge the absolute value of acid number and the adjacent last hypo acid value difference measured in above-mentioned steps S6, if this absolute value > is 0.5mgKOH/g, then return step S5; If this absolute value≤0.5mgKOH/g, then enter next step;
step S8:if acid number is > 1.5mgKOH/g still, then terminate this lab scale, and return step S2 and again adjust in the scope of 0.9:n ~ 1.2:n and set once the concrete mol ratio that amyl-based polyol and enanthic acid lab scale test; If acid number≤1.5mgKOH/g, then enter next step;
step S9:in three-necked bottle, add amyl-based polyol used or mix new penta season polyvalent alcohol and enanthic acid always feed intake quality 0.5 ~ 5%, particle diameter is the adsorption decolouriser of 65 ~ 80 μm, continue heated and stirred 0.5 ~ 2h, then heating is stopped, when being cooled to 50 ~ 70 DEG C in lab scale sample, in the Büchner funnel being covered with middling speed quantitative paper, carry out suction filtration while hot, the product in filter flask is transferred in reagent bottle;
step S10:according to the method that GB/T 7305-2003 specifies, synthesis liquid in mensuration reagent bottle and the separation property of water, if be less than 3mL at the volume of the three ten minutes internal emulsification layers left standstill after the result display high-speed stirring recorded terminates, then represent that the separation property of this synthesis liquid and water is good, terminate this lab scale, write down this batch of enanthic acid used and the suitable mol ratio of amyl-based polyol, using the mol ratio of this lab scale as proportioning raw materials when carrying out large-scale production with the raw material of present lot; If measurement result display synthesis liquid and the separation property of water bad, then return step S2, in the test of fine setting lab scale enanthic acid and amyl-based polyol or mix new penta season polyvalent alcohol concrete mol ratio, then carry out lab scale next time;
step S11:large-scale production.
3. the preparation technology of amyl-based polyol heptanoate according to claim 1 and 2, is characterized in that the step of described large-scale production is specially:
step S111:the present lot obtained with lab scale amyl-based polyol used or mix new penta season polyvalent alcohol and the mol ratio of enanthic acid, at 2M
3reactor in, drop into enanthic acid and amyl-based polyol or mix new penta season polyvalent alcohol, the total mass of raw material in still is made to be in the scope of 500 ~ 1500kg, open and stir, during beginning, rotating speed maintains 5 ~ 50rpm, open the heating valve of reactor, material in still is heated, when temperature in the kettle is raised to 115 ± 5 DEG C, add enanthic acid and amyl-based polyol used or mix new penta season polyvalent alcohol always feed intake quality 0.5 ~ 2% tosic acid as catalyzer, open nitrogen valve, nitrogen is passed into the flow velocity of 1 ~ 100L/min, the rotating speed of stirring is brought up to 50 ~ 300rpm, timing from now, material in still is warmed up to 120 ~ 250 DEG C, heating 5 ~ 24h, the water of observing response by-product is deviate to the speed conditions in collection device under the drive of nitrogen, by the time no longer included after a water deviates from collection device in 5 ~ 20 minutes, sampling, the acid number of working sample,
step S112:if the acid number of sample can not reach≤level of 1.5mgKOH/g, then carry out reaction 0.5 ~ 2h, resampling detects acid number, until the acid number≤1.5mgKOH/g of sample;
step S113:in reactor, add amyl-based polyol used or mix new penta season polyvalent alcohol and enanthic acid always feed intake quality 0.1 ~ 2% adsorption decolouriser, continue heated and stirred 0.5 ~ 3h, then heating is stopped, when being cooled to 50 ~ 70 DEG C Deng the temperature of product in still, open the valve at the bottom of still, with refining filtering pump by flow out material pumping in pressure filter, order number is adopted to be 250 ~ 300 object filter screens, carry out circulation press filtration, press filtration material out turns back in reactor, the color that circulation press filtration proceeds to the product returned do not seen adsorption decolouriser particle residual till, product after press filtration being decoloured pours in pail pack.
4. the preparation technology of amyl-based polyol heptanoate according to claim 1 and 2, is characterized in that: described amyl-based polyol or mix new penta season polyvalent alcohol be one or more in TriMethylolPropane(TMP), ditrimethylolpropane, tetramethylolmethane, dipentaerythritol, neopentyl glycol.
5. the preparation technology of amyl-based polyol heptanoate according to claim 3, is characterized in that: described amyl-based polyol or mix new penta season polyvalent alcohol be one or more in TriMethylolPropane(TMP), ditrimethylolpropane, tetramethylolmethane, dipentaerythritol, neopentyl glycol.
6. the preparation technology of amyl-based polyol heptanoate according to claim 2, is characterized in that: described adsorption decolouriser can be gac, atlapulgite, attapulgite, diatomite.
7. the preparation technology of amyl-based polyol heptanoate according to claim 3, is characterized in that: described adsorption decolouriser can be gac, atlapulgite, attapulgite, diatomite.
8. the preparation technology of the amyl-based polyol heptanoate according to claim 6 or 7, is characterized in that: when described adsorption decolouriser is gac, can use together in conjunction with diatomite, attapulgite, atlapulgite.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510370888.2A CN105017014A (en) | 2015-06-30 | 2015-06-30 | Preparation method of neo-pentyl polyhydric alcohol heptanoic acid ester |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510370888.2A CN105017014A (en) | 2015-06-30 | 2015-06-30 | Preparation method of neo-pentyl polyhydric alcohol heptanoic acid ester |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105017014A true CN105017014A (en) | 2015-11-04 |
Family
ID=54407377
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510370888.2A Pending CN105017014A (en) | 2015-06-30 | 2015-06-30 | Preparation method of neo-pentyl polyhydric alcohol heptanoic acid ester |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105017014A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112559577A (en) * | 2020-12-15 | 2021-03-26 | 苏州千木信息技术有限公司 | Recommendation method and system for plate processing technology |
-
2015
- 2015-06-30 CN CN201510370888.2A patent/CN105017014A/en active Pending
Non-Patent Citations (4)
| Title |
|---|
| 秦中秋: "三羟甲基丙烷三异辛酯合成工艺研究", 《辽宁化工》 * |
| 费建奇; 赵伟: "新戊基多元醇脂肪酸的酯化反应机理与酯的结构设计", 《润滑油》 * |
| 费建奇; 赵伟: "硫酸催化新戊基多元醇脂肪酸酯化反应行为研究", 《润滑油》 * |
| 邢凤兰; 马文辉; 徐群; 刘范嘉: "三羟甲基丙烷酯的合成及其抗乳化性能研究", 《化工进展》 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112559577A (en) * | 2020-12-15 | 2021-03-26 | 苏州千木信息技术有限公司 | Recommendation method and system for plate processing technology |
| CN112559577B (en) * | 2020-12-15 | 2024-04-30 | 苏州千木信息技术有限公司 | Method and system for recommending plate processing technology |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104945247A (en) | Preparation process of neopentyl polyol oleate | |
| Roschat et al. | Biodiesel production based on heterogeneous process catalyzed by solid waste coral fragment | |
| Liu et al. | Transesterification of poultry fat with methanol using Mg–Al hydrotalcite derived catalysts | |
| US20050016059A1 (en) | Method for transesterifyng vegetable oils | |
| CN103073712A (en) | Preparation method for polyester by using liquid titanium catalyst | |
| CN105793228A (en) | Hydrogenation method of phthalate compound | |
| CN101538228A (en) | Method for synthesizing medical compound peramivir for resisting influenza viruses and avian influenza viruses | |
| CN101805270B (en) | Aliphatic diisocyanate and preparation method and purposes thereof | |
| CN105130800A (en) | Preparation technology for mixed-acid neo-pentyl polyol ester | |
| Liu et al. | Transesterification of soybean oil using CsF/CaO catalysts | |
| CN103965040B (en) | A kind of method of preparing dibasic acid dimethyl ester | |
| TW201527275A (en) | Process | |
| CN105017014A (en) | Preparation method of neo-pentyl polyhydric alcohol heptanoic acid ester | |
| CN104822643B (en) | Hydrogenated products from biologically-derived carboxylate | |
| CN103319341A (en) | Method for synthesizing methyl oleate | |
| CN104926654A (en) | 2-ethylhexoic acid neopentyl polyol ester preparation technology | |
| CN105037145A (en) | Process for preparing neo-polyhydric alcohol aliphatic ester by adopting prepared acid | |
| CN105001082A (en) | Preparation technology of neopentyl polyol laurate | |
| CN101773846A (en) | Loaded solid alkali zeolite catalyst for synthesizing long-chain alkyl carbonate | |
| CN105037146A (en) | Di-trimethylolpropane laurate and preparation method thereof | |
| CN104910010A (en) | Method for producing di-trimethylolpropane heptylate | |
| CN109134249A (en) | A kind of preparation method of isopropyl fatty acid ester | |
| CN105037144A (en) | 2-ethylexanoic acid bi-trimethylolpropane ester and production method thereof | |
| CN1970529A (en) | Cardiovascular drug acebutolol intermediate 2- acetyl-4-n-butyramidophenol synthesis method | |
| CN105130799A (en) | Method for producing di(trimethylolpropane) trioleate |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20151104 |
|
| RJ01 | Rejection of invention patent application after publication |