CN115487855A - Preparation method of catalyst for preparing polyol fatty acid ester - Google Patents
Preparation method of catalyst for preparing polyol fatty acid ester Download PDFInfo
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
- B01J29/405—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing rare earth elements, titanium, zirconium, hafnium, zinc, cadmium, mercury, gallium, indium, thallium, tin or lead
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/03—Catalysts comprising molecular sieves not having base-exchange properties
- B01J29/0308—Mesoporous materials not having base exchange properties, e.g. Si-MCM-41
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/041—Mesoporous materials having base exchange properties, e.g. Si/Al-MCM-41
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/10—After treatment, characterised by the effect to be obtained
- B01J2229/20—After treatment, characterised by the effect to be obtained to introduce other elements in the catalyst composition comprising the molecular sieve, but not specially in or on the molecular sieve itself
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Abstract
The invention provides a catalyst for preparing polyol fatty acid ester, which is SO taking a molecular sieve as a carrier 4 2‑ /TiO 2 ‑M x O y Catalysts of type (I) in which M x O y Is a metal oxide. The preparation method of the catalyst comprises the following steps: pretreating the molecular sieveAdding the molecular sieve into the composite metal salt solution, and adjusting the pH value of the mixed solution to 8-10; aging the precipitate in the mixed solution, filtering, washing the filter cake, and drying the filter cake; grinding the solid into powder after drying, and then soaking the ground powder into ammonium persulfate; and filtering after the impregnation is finished, drying a filter cake, roasting, and obtaining the catalyst after the roasting is finished. The invention also provides a method for preparing the polyol fatty acid ester by using the catalyst. The catalyst can be repeatedly used, the cycle stability is very good, and the properties of the catalytic synthesis product in all aspects are superior to those of the catalytic synthesis product of the traditional catalyst.
Description
Technical Field
The invention relates to the technical field of chemical synthesis, in particular to a preparation method of a catalyst for preparing polyol fatty acid ester.
Background
Along with the development of economy, the degree of industrialization is continuously deepened, and people pay more and more attention to the pollution of the production and use of industrial products to the environment. In the lubricating oil industry, the requirements on the use performance, biodegradability, low toxicity or non-toxicity and the like of lubricating oil are higher and higher, the traditional mineral-based lubricating oil is difficult to meet the harsh requirements, and the development trend of the lubricating oil is energy conservation, environmental protection and long service life.
The polyol ester is used as one of group V base oils, has excellent properties in all aspects such as viscosity-temperature performance, thermal oxidation stability and the like, has low evaporation loss, is biodegradable, and is widely used in the field of lubricating oils such as flame-retardant hydraulic oil, chain saw oil and the like.
Chinese patent application document CN101475467 reports a new process for synthesizing polyol ester by using immobilized lipase to catalyze transesterification reaction between fatty acid lower ester and neopentyl polyol, which has the advantages of low cost and high transesterification yield, but the quality indexes of the product such as acid value, hydroxyl value and the like are not mentioned, and the properties of the product cannot be completely evaluated. In addition, lipase is easy to be poisoned and inactivated, and is difficult to be applied in industry. Chinese patent application CN101456813 reports a method for synthesizing polyol ester with functionalized ionic liquid as a catalyst, which has relatively mild conditions, high esterification rate, stable catalyst and recycling capability, but the ionic liquid type catalyst has high cost, and the use of the catalyst is limited more, and is difficult to apply. Chinese patent application publication CN112574029 reports the use of SO 4 2- /M x O y The preparation method of the solid super acidic polyol ester has the advantages that after most of the reaction, acid is removed by combining reduced pressure distillation and molecular distillation, the product has better indexes in all aspects, and the three wastes are less.
The polyol fatty acid ester can be obtained by directly esterifying polyol and fatty acid under the action of an acid catalyst or by carrying out transesterification on polyol and fatty acid methyl ester, but the transesterification method has the disadvantages of more waste and complicated process, the direct esterification method is generally taken as the main industrial production, the catalyst used in the direct esterification method is generally concentrated sulfuric acid, methanesulfonic acid and other protonic acids, and then the product is refined by the steps of catalyst separation, deacidification, decoloration and the like. The catalyst has high corrosion to equipment, is difficult to separate, has a complex process, and produces products with high chroma and poor quality. Therefore, the problem to be solved is how to provide a new catalyst which can be recycled and a preparation method of polyol fatty acid ester which has simple process, low acid value of the product and low color of the product.
Disclosure of Invention
Aiming at the defects existing in the problems, the invention provides a catalyst for preparing polyol fatty acid ester, which is SO taking a molecular sieve as a carrier 4 2- /TiO 2 -M x O y Catalyst of type (I) in which M x O y Is a metal oxide.
As a further improvement of the invention, M x O y Is selected from: fe 2 O 3 、Al 2 O 3 、La 2 O 3 、CeO 2 、 ZrO 2 One or more of (a).
The present invention also provides a method for preparing a catalyst for the preparation of polyol fatty acid esters, which comprises the steps of:
step A, pretreating a molecular sieve, adding the treated molecular sieve into a composite metal salt solution, and adjusting the pH value of the mixed solution to 8-10;
b, ageing the precipitate in the mixed solution in the step A, filtering, washing a filter cake, and drying the filter cake;
step C, grinding the solid into powder after drying, and then soaking the ground powder into ammonium peroxodisulfate;
and D, filtering after the impregnation is finished, drying a filter cake, and roasting to obtain the catalyst.
As a further improvement of the invention, in the step A, the molecular sieve is roasted for 2 to 6 hours at the temperature of 300 to 500 ℃ for pretreatment, the treated molecular sieve is added into a composite metal salt solution, and 10 percent of sodium hydroxide aqueous solution is dripped into the system to adjust the pH value to 8 to 10.
As a further improvement of the invention, in the step B, the precipitate obtained in the step A is aged at the temperature of 5-20 ℃ for 12-20h, filtered, the filter cake is washed by ethanol and deionized water, and the filter cake is dried at the temperature of 80-120 ℃ for 2-8h.
As a further improvement of the invention, the solid is ground into powder of 80-100 meshes after being dried in the step C, and the ground powder is soaked in ammonium peroxodisulfate with the concentration of 0.5-1mol/L for 5-12h.
And D, filtering after the impregnation is finished in the step D, drying a filter cake in a drying oven at the temperature of 60-100 ℃, and finally roasting at the roasting temperature of 400-600 ℃ for 2-6h to obtain the catalyst after the roasting is finished.
As a further improvement of the invention, the molecular sieve is selected from the group consisting of: MCM-41, HZSM-5 or SBA-15.
As a further improvement of the invention, the composite metal salt solution comprises titanium sulfate, and the composite metal salt solution also comprises: one or more of zirconium nitrate, aluminum nitrate, ferric sulfate, cerium nitrate or lanthanum nitrate.
As a further improvement of the invention, the molar ratio of the silicon element in the molecular sieve to the metal element in the composite metal salt solution is 8.
As a further improvement of the invention, the concentration of the titanium sulfate contained in the composite metal salt solution is 0.1-0.4mol/L.
The invention also provides a preparation method of the polyol fatty acid ester. The preparation method comprises the following steps:
step one, under the protection of inert gas, adding polyalcohol, fatty acid and the catalyst of any one of claims 1 or 2 into a reactor with a water-dividing device;
step two, heating to 160-180 ℃ and reacting for 4-6h;
step three, continuously heating to 180-230 ℃, reacting for 6-12h, and stopping the reaction when the acid value of the reaction solution is detected to be less than or equal to 2 mgKOH/g;
and step four, standing the reaction liquid obtained in the step three, filtering the reaction liquid, taking a filter cake as a catalyst, recycling the catalyst, and performing molecular distillation on the filtrate to obtain the polyol fatty acid ester.
As a further improvement of the invention, the molar ratio of hydroxyl groups to carboxyl groups in the polyol and fatty acid is 1.
As a further improvement of the invention, the polyol is selected from: one or more of neopentyl glycol, trimethylolpropane, pentaerythritol or dipentaerythritol; the fatty acid is selected from: c 6 -C 12 One or both of linear or branched fatty acids.
As a further improvement of the invention, the evaporation temperature in molecular distillation is 170-200 ℃, the vacuum degree is 5-30pa, and the obtained heavy phase distillate is polyol fatty acid ester.
Compared with the prior art, the invention has the beneficial effects that:
1. the catalyst provided by the invention introduces the molecular sieve to modify the solid super acid, and increases the specific surface area and the active center of the catalyst, thereby improving the catalytic efficiency.
2. The preparation method of the polyol fatty acid ester provided by the invention avoids the change of product color caused by high-temperature vacuum deacidification in the post-treatment process, and also avoids the generation of a large amount of waste water and waste liquid in alkali washing.
3. The polyol fatty acid ester prepared by the method has the advantages of low acid value and low chroma.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the embodiments of the present invention, and it is obvious that the described embodiments are part of the embodiments of the present invention, but not all of the embodiments. All other embodiments, which can be obtained by a person skilled in the art without making any creative effort based on the embodiments in the present invention, belong to the protection scope of the present invention.
EXAMPLE one preparation of the catalyst
Putting the HZSM-5 molecular sieve into a muffle furnace to be roasted for 3h at the temperature of 400 ℃, taking out 50g of the HZSM-5 molecular sieve, adding the HZSM-5 molecular sieve into 500ml of 0.4mol/L titanium sulfate solution, quickly dropwise adding a sodium hydroxide aqueous solution with the mass fraction of 10%, and adjusting the pH value to 8. Precipitates appear in the mixed solution, and the precipitates are aged for 12 hours at the temperature of 20 ℃. After filtration, the filter cake is washed by ethanol and deionized water and is dried for 6 hours in an oven at 80 ℃. After drying, the solid was ground to 80 mesh. Soaking the solid powder in 0.5mol/L ammonium peroxodisulfate for 10h, filtering, and drying in an oven at 100 deg.C for 3h. And (4) after drying, roasting for 3 hours at 550 ℃ by using a muffle furnace to obtain the catalyst.
EXAMPLE II preparation of polyol fatty acid esters
A1000 ml four-necked flask was charged with 93.92g (0.70 mol) of trimethylolpropane, 621.41g (2.20 mol) of oleic acid and 21.5g of the catalyst prepared in example one, and a water separator was installed. The flask was replaced with nitrogen three times, after which the nitrogen flow rate was maintained at 20mL/min. The temperature is increased to 160 ℃ at first, the temperature is increased to 160 ℃, the nitrogen flow rate is kept at 200mL/min, and the reaction is carried out for 6h. The temperature is continuously increased to 230 ℃, the reaction is carried out for 10 hours, and the acid value of the product is sampled and tested to be 1.64mgKOH/g. Cooling the reaction liquid to room temperature, standing, filtering the reaction liquid, recycling the catalyst obtained by separation, and performing molecular distillation on the crude filtrate at 160 ℃ and under the vacuum degree of 10pa, wherein the heavy-phase distillate is a trimethylolpropane oleate product, and the light-phase distillate is oleic acid. The molecular distillation is carried out for one time, and then the filtration is carried out to obtain the finished product. The sample had an acid value of 0.23mgKOH/g, an ASTM color value of less than 0.5, and a pale yellow appearance.
EXAMPLE III preparation of the catalyst
The MCM-41 molecular sieve is placed into a muffle furnace to be roasted for 2 hours at the temperature of 500 ℃, 50g of the MCM-41 molecular sieve is taken out and added into 500ml of a mixed solution of 0.3mol/L titanium sulfate and 0.1mol/L zirconium nitrate, a sodium hydroxide aqueous solution with the mass fraction of 10% is quickly dripped, and the pH value is adjusted to 9. Precipitates appear in the mixed solution, and the precipitates are aged for 12 hours at the temperature of 5 ℃. After filtration, the solid was washed with ethanol and deionized water and dried in an oven at 100 ℃ for 2h. After drying, the solid was ground to 80 mesh. The solid powder is immersed in 0.75mol/L ammonium peroxodisulfate for 8h, filtered, and dried in an oven at 100 ℃ for 3h. And (3) drying, and roasting for 3 hours at 500 ℃ by using a muffle furnace to obtain the catalyst.
EXAMPLE four preparation of polyol fatty acid esters
A1000 ml four-necked flask was charged with 62.5g (0.60 mol) of neopentyl glycol, 355.9g (1.26 mol) of oleic acid and 12.0g of the catalyst prepared in example III, and equipped with a water-dividing device. The flask was replaced with nitrogen three times, after which the nitrogen flow rate was maintained at 10mL/min. The temperature is increased to 160 ℃, the nitrogen flow rate is 100mL/min after the temperature is increased to 160 ℃, and the reaction is carried out for 4h. The temperature is continuously increased to 200 ℃, the reaction is carried out for 8h, the acid value of the product is sampled and tested to be 1.73mgKOH/g, and the reaction liquid is cooled to the room temperature. Standing, filtering the reaction solution, recovering the separated catalyst, and performing molecular distillation on the filtrate at 160 ℃ and under the vacuum degree of 10pa, wherein the heavy-phase distillate is a pentaerythritol oleate product, and the light-phase distillate is oleic acid. The molecular distillation is carried out for one-time separation and then the filtration is carried out to obtain the finished product. The product has an acid value of 0.14mgKOH/g, an ASTM color value of less than 0.5 and a light yellow appearance.
EXAMPLE V preparation of the catalyst
Placing the HZSM-5 molecular sieve into a muffle furnace to be roasted for 3 hours at the temperature of 400 ℃, taking out 50g of the HZSM-5 molecular sieve, adding the HZSM-5 molecular sieve into 500ml of 0.4mol/L titanium sulfate solution, quickly dropwise adding a sodium hydroxide aqueous solution with the mass fraction of 10%, and adjusting the pH value to 8. Precipitates appear in the mixed solution, and the precipitates are aged for 12 hours at the temperature of 10 ℃. After filtration, the solid was washed with ethanol and deionized water and dried in an oven at 120 ℃ for 2h. After drying, the solid was ground to 80 mesh. The solid powder was immersed in 0.75mol/L ammonium peroxodisulfate for 5h, filtered, and dried in an oven at 100 ℃ for 3h. And (4) after drying, roasting for 3 hours at 550 ℃ by using a muffle furnace to obtain the catalyst.
EXAMPLE sixthly preparation of polyol fatty acid esters
A1000 ml four-necked flask was charged with 108.9g (0.80 mol) of pentaerythritol, 337.4g (3.24 mol) of octanoic acid and 17.85g of the catalyst prepared in example five, and equipped with a water separator. The flask was replaced with nitrogen three times, after which the nitrogen flow rate was maintained at 20mL/min. The temperature is increased to 160 ℃ and then the reaction is carried out for 6h after the temperature is increased to 160 ℃. And continuously heating to 200 ℃, controlling the nitrogen flow rate to be 400mL/min, reacting for 12h, sampling to test the acid value of the product to be 1.98mgKOH/g, and cooling the reaction liquid to room temperature. Standing, filtering the reaction solution, recovering the separated catalyst, and performing molecular distillation on the filtrate at 180 ℃ and under the vacuum degree of 10pa, wherein the heavy-phase distillate is a pentaerythritol caprylate product, and the light-phase distillate is caprylic acid. The molecular distillation is carried out for one-time separation and then the filtration is carried out to obtain the finished product. The sample had an acid value of 0.09mgKOH/g, an ASTM color value of less than 0.5, and a pale yellow appearance.
Comparative example I preparation of polyol fatty acid ester
A1000 ml four-necked flask was charged with 93.92g (0.70 mol) of trimethylolpropane, 621.41g (2.20 mol) of oleic acid, and 21.5g of a p-toluenesulfonic acid catalyst, and a water separator was attached. The flask was replaced with nitrogen three times, after which the nitrogen flow rate was maintained at 20mL/min. The temperature is increased to 160 ℃, the nitrogen flow rate is kept at 200mL/min after the temperature is increased to 160 ℃, and the reaction is carried out for 6h. The temperature is increased to 230 ℃ continuously, the reaction is carried out for 15h, and a sample is taken to test the acid value of the product to be 4.23mgKOH/g. The reaction was cooled to room temperature. The catalyst can not be recycled, the post-treatment is complex, the acid value of the treated sample is 0.89mgKOH/g, the chroma is dark, the appearance is brown yellow, and the quality is poor.
Evaluation data of the polyol fatty acid esters obtained in comparative example one and examples two, four and six are shown in Table 1.
TABLE 1
| Detecting items | Comparative example 1 | Example two | Example four | EXAMPLE six | Detection method |
| Chroma (ASTM) | 1.9 | ＜0.5 | ＜0.5 | ＜0.5 | GB/T 6540 |
| Viscosity, 40 ℃ C., mm 2 /s | 46.88 | 45.62 | 24.96 | 30.92 | GB/T 265 |
| Viscosity, 100 ℃ mm 2 /s | 9.69 | 9.50 | 6.02 | 7.07 | GB/T 265 |
| Viscosity index | 198 | 199 | 203 | 202 | GB/T 1995 |
| Acid value of mgKOH/g | 0.89 | 0.23 | 0.14 | 0.09 | GB/T 9104 |
| Hydroxyl value, mgKOH/g | 8.9 | 3.9 | 3.81 | 4.85 | GB/T 7383 |
| Water content% | 0.05 | 0.03 | 0.02 | 0.03 | GB/T 260 |
EXAMPLE seventhly, stability test of catalyst
A1000 ml four-necked flask was charged with 80.5g (0.60 mol) of trimethylolpropane, 508.43g (1.80 mol) of oleic acid and 17.7g of the catalyst prepared in example one, and a water separator was attached. The flask was replaced with nitrogen three times, after which the nitrogen flow rate was maintained at 20mL/min. The temperature is increased to 160 ℃ at first, the temperature is increased to 160 ℃, the nitrogen flow rate is kept at 200mL/min, and the reaction is carried out for 6h. The temperature is continuously increased to 230 ℃, the reaction is carried out for 8 hours, and a sample is taken to test the acid value of the product. And cooling the reaction liquid to room temperature, standing, filtering the reaction liquid, measuring the esterification rate in the filtrate, and recovering and reusing the catalyst obtained by separation. The recovered catalyst was further reacted according to the reaction conditions in example seven.
The catalyst was reused 18 times as described above and the results of the catalyst stability test are shown in table 2.
TABLE 2
| Number of experiments | 1 | 2 | 3 | 4 | 5 | 6 | 7 | 8 | 9 |
| Degree of esterification/%) | 99.6 | 99.5 | 99.6 | 99.5 | 99.5 | 99.7 | 99.8 | 99.7 | 99.7 |
| Number of experiments | 10 | 11 | 12 | 13 | 14 | 15 | 16 | 17 | 18 |
| Degree of esterification/%) | 99.6 | 99.5 | 99.6 | 99.5 | 99.1 | 99.6 | 99.5 | 99.6 | 99.5 |
And (4) conclusion:
1. the catalyst provided by the invention has very good cycle stability, and the esterification rate of the product obtained by catalysis after the catalyst is recycled for 18 times is still more than 99%.
2. The catalyst provided by the invention introduces the molecular sieve to modify the solid super acid, and increases the specific surface area and the active center of the catalyst, thereby improving the catalytic efficiency.
3. The preparation method of the polyol fatty acid ester provided by the invention avoids the change of product color caused by high-temperature vacuum deacidification in the post-treatment process, and also avoids the generation of a large amount of waste water and waste liquid in alkali washing.
4. The polyol fatty acid ester prepared by the method has the advantages of low acid value and low chroma.
The present invention has been described in terms of the preferred embodiment, and it is not intended to be limited to the embodiment. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. The catalyst for preparing the polyol fatty acid ester is characterized in that the catalyst is SO taking a molecular sieve as a carrier 4 2- /TiO 2 -M x O y Catalyst of type (I) in which M x O y Is a metal oxide.
2. The catalyst of claim 1, wherein M is x O y Is selected from: fe 2 O 3 、Al 2 O 3 、La 2 O 3 、CeO 2 、ZrO 2 One or more of (a).
3. A preparation method of a catalyst for preparing polyol fatty acid ester is characterized by comprising the following steps:
step A, pretreating a molecular sieve, adding the treated molecular sieve into a composite metal salt solution, and adjusting the pH value of the mixed solution to 8-10;
b, ageing the precipitate in the mixed solution in the step A, filtering, washing a filter cake, and drying the filter cake;
step C, grinding the solid into powder after drying, and then soaking the ground powder into ammonium peroxodisulfate;
and D, filtering after the impregnation is finished, drying a filter cake, and roasting to obtain the catalyst.
4. The production method according to claim 3,
in the step A, the molecular sieve is roasted for 2-6h at the temperature of 300-500 ℃ for pretreatment, the treated molecular sieve is added into a composite metal salt solution, and 10% sodium hydroxide aqueous solution is dripped into the system to adjust the pH value to 8-10;
in the step B, the precipitate obtained in the step A is aged at the temperature of 5-20 ℃ for 12-20h, filtered, the filter cake is washed by ethanol and deionized water, and dried at the temperature of 80-120 ℃ for 2-8h;
grinding the solid into powder of 80-100 meshes after drying in the step C, and then soaking the ground powder into ammonium peroxydisulfate with the concentration of 0.5-1mol/L for 5-12h;
and D, filtering after the impregnation is finished, drying the filter cake in an oven at the temperature of 60-100 ℃, and finally roasting at the roasting temperature of 400-600 ℃ for 2-6h to obtain the catalyst after the roasting is finished.
5. The method of claim 3, wherein the molecular sieve is selected from the group consisting of: MCM-41, HZSM-5 or SBA-15.
6. The method for preparing the alloy material according to claim 3, wherein the complex metal salt solution comprises titanium sulfate, and the complex metal salt solution further comprises: one or more of zirconium nitrate, aluminum nitrate, ferric sulfate, cerium nitrate or lanthanum nitrate.
7. The method according to claim 3, wherein the molar ratio of the silicon element in the molecular sieve to the metal element in the composite metal salt solution is 8.
8. The method of claim 3, wherein the concentration of titanium sulfate included in the complex metal salt solution is 0.1 to 0.4mol/L.
9. A preparation method of polyol fatty acid ester is characterized by comprising the following steps:
step one, under the protection of inert gas, adding polyalcohol, fatty acid and the catalyst of any one of claims 1 or 2 into a reactor with a water-dividing device;
step two, heating to 160-180 ℃ and reacting for 4-6h;
step three, continuously heating to 180-230 ℃, reacting for 6-12h, and stopping the reaction when the acid value of the reaction solution is detected to be less than or equal to 2 mgKOH/g;
and step four, standing the reaction liquid obtained in the step three, filtering the reaction liquid, taking a filter cake as a catalyst, recycling the catalyst, and performing molecular distillation on the filtrate to obtain the polyol fatty acid ester.
10. The process according to claim 9, wherein the molar ratio of hydroxyl groups to carboxyl groups in the polyol and fatty acid is 1;
the polyol is selected from: one or more of neopentyl glycol, trimethylolpropane, pentaerythritol or dipentaerythritol; the fatty acid is selected from: c 6 -C 12 One or both of linear or branched fatty acids;
the evaporation temperature in the molecular distillation is 170-200 ℃, the vacuum degree is 5-30pa, and the obtained heavy phase distillate is polyol fatty acid ester.
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