CN112980488A - High-acid-value grease non-catalytic esterification and distillation synchronous deacidification process - Google Patents
High-acid-value grease non-catalytic esterification and distillation synchronous deacidification process Download PDFInfo
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- CN112980488A CN112980488A CN202110213057.XA CN202110213057A CN112980488A CN 112980488 A CN112980488 A CN 112980488A CN 202110213057 A CN202110213057 A CN 202110213057A CN 112980488 A CN112980488 A CN 112980488A
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- grease
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- 239000002253 acid Substances 0.000 title claims abstract description 53
- 239000004519 grease Substances 0.000 title claims abstract description 41
- 238000005886 esterification reaction Methods 0.000 title claims abstract description 29
- 230000032050 esterification Effects 0.000 title claims abstract description 28
- 238000000034 method Methods 0.000 title claims abstract description 28
- 238000004821 distillation Methods 0.000 title claims abstract description 25
- 230000008569 process Effects 0.000 title claims abstract description 18
- 230000001360 synchronised effect Effects 0.000 title claims abstract description 14
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 10
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 claims abstract description 103
- 238000006243 chemical reaction Methods 0.000 claims abstract description 40
- 235000014113 dietary fatty acids Nutrition 0.000 claims abstract description 22
- 229930195729 fatty acid Natural products 0.000 claims abstract description 22
- 239000000194 fatty acid Substances 0.000 claims abstract description 22
- 150000004665 fatty acids Chemical class 0.000 claims abstract description 17
- 238000010438 heat treatment Methods 0.000 claims abstract description 16
- 239000002994 raw material Substances 0.000 claims abstract description 16
- 125000005456 glyceride group Chemical group 0.000 claims abstract description 10
- 238000001816 cooling Methods 0.000 claims abstract description 8
- 238000007599 discharging Methods 0.000 claims abstract description 8
- 238000003756 stirring Methods 0.000 claims abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 5
- 238000001914 filtration Methods 0.000 claims abstract description 3
- 239000003921 oil Substances 0.000 claims description 26
- 239000008162 cooking oil Substances 0.000 claims description 7
- 238000005070 sampling Methods 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims description 2
- 235000011187 glycerol Nutrition 0.000 abstract description 37
- 238000010924 continuous production Methods 0.000 abstract description 4
- 230000035484 reaction time Effects 0.000 abstract description 3
- 235000019198 oils Nutrition 0.000 description 25
- 238000006297 dehydration reaction Methods 0.000 description 15
- 239000000047 product Substances 0.000 description 11
- 239000003225 biodiesel Substances 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 238000003860 storage Methods 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 4
- 230000018044 dehydration Effects 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000000813 microbial effect Effects 0.000 description 3
- 239000003549 soybean oil Substances 0.000 description 3
- 235000012424 soybean oil Nutrition 0.000 description 3
- 241000723422 Catalpa Species 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 235000019484 Rapeseed oil Nutrition 0.000 description 2
- -1 alcohol ester Chemical class 0.000 description 2
- 238000009874 alkali refining Methods 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000004904 shortening Methods 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- QIIDATRCGITYRZ-UHFFFAOYSA-N Catalpol Natural products OCC1OC(OC2OC=CC3C(O)C(=C(CO)C23)O)C(O)C(O)C1O QIIDATRCGITYRZ-UHFFFAOYSA-N 0.000 description 1
- 235000021355 Stearic acid Nutrition 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- LHDWRKICQLTVDL-PZYDOOQISA-N catalpol Chemical compound O[C@@H]1[C@@H](O)[C@H](O)[C@@H](CO)O[C@H]1O[C@H]1[C@@H]2[C@@]3(CO)O[C@H]3[C@@H](O)[C@@H]2C=CO1 LHDWRKICQLTVDL-PZYDOOQISA-N 0.000 description 1
- UXSACQOOWZMGSE-UHFFFAOYSA-N catalposide Natural products OC1C(O)C(O)C(CO)OC1OC1C2C3(CO)OC3C(OC(=O)C=3C=CC(O)=CC=3)C2C=CO1 UXSACQOOWZMGSE-UHFFFAOYSA-N 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 235000005687 corn oil Nutrition 0.000 description 1
- 239000002285 corn oil Substances 0.000 description 1
- 238000006114 decarboxylation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000010494 dissociation reaction Methods 0.000 description 1
- 230000005593 dissociations Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 235000021588 free fatty acids Nutrition 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- LHDWRKICQLTVDL-UHFFFAOYSA-N methyl iridoid glycoside Natural products OC1C(O)C(O)C(CO)OC1OC1C2C3(CO)OC3C(O)C2C=CO1 LHDWRKICQLTVDL-UHFFFAOYSA-N 0.000 description 1
- QIQXTHQIDYTFRH-UHFFFAOYSA-N octadecanoic acid Chemical compound CCCCCCCCCCCCCCCCCC(O)=O QIQXTHQIDYTFRH-UHFFFAOYSA-N 0.000 description 1
- OQCDKBAXFALNLD-UHFFFAOYSA-N octadecanoic acid Natural products CCCCCCCC(C)CCCCCCCCC(O)=O OQCDKBAXFALNLD-UHFFFAOYSA-N 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000008117 stearic acid Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 239000002383 tung oil Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/42—Catalytic treatment
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Fats And Perfumes (AREA)
Abstract
The invention relates to a non-catalytic esterification and distillation synchronous deacidification process for high-acid-value grease. The method can synchronously realize the esterification and distillation removal of fatty acid in grease, and quickly realize the purpose of reducing acid value with low loss. The method is characterized in that: adopting high-acid-value grease and glycerol as raw materials, filtering the grease, dehydrating, degumming and the like, and then adding the glycerol; stirring and heating to react under vacuum; then heating for reaction; and finally, controlling the temperature to be 220-240 ℃, ensuring the pressure to be lower than 0.02MPa, injecting glycerin or water vapor from the bottom of the reaction kettle, and distilling and deacidifying while esterifying. When the distillate is basically not available, the reaction is stopped, and the fatty glyceride product with low acid value can be obtained after cooling and discharging. The invention can directly prepare high-purity fatty glyceride from high-acid-value grease without improving the existing equipment, can effectively reduce the acid value, shorten the reaction time and improve the quality of the esterification product. Realizing 'zero loss' in continuous production.
Description
Technical Field
The invention relates to a non-catalytic esterification and distillation synchronous deacidification process for high-acid-value grease, belonging to the fields of chemical utilization of grease, new energy and related equipment.
Background
Biodiesel (fatty acid lower alcohol ester) is a novel environment-friendly fuel with molecular weight very close to that of the existing diesel, and raw materials are derived from various renewable oils (such as soybean oil, rapeseed oil, catalpol oil, microbial oil, illegal cooking oil and the like). Although the fatty acid ester biodiesel has the advantages of wide raw material source, excellent use performance, high environmental protection performance, good engine starting performance, renewability and the like; and the vigorous development of the biodiesel has important significance for energy safety, air pollution prevention, environmental improvement, economic sustainable development and the like. However, many bottleneck problems are encountered in the actual operation, such as: most of the grease capable of preparing the biodiesel is edible grease, such as soybean oil, corn oil, rapeseed oil and the like, and the problem of food competition with people exists; in addition, the woody grease such as catalpa oil, tung oil and the like basically has respective industries and is higher in cost when used for synthesizing special materials; the microbial oil has not only insufficient yield, but also has the problem of cost; although the price of the illegal cooking oil, the acidified oil and the like is not high, the quality of the oil product is not good, and the oil product needs to be further processed for use. Therefore, how to reduce the cost of the biodiesel raw material always restricts the development of the industry and is a problem which needs to be solved urgently by the market.
The price influence factors of the soybean oil, the catalpa oil, the microbial oil and the like are fixed and are difficult to reduce. Only high acid value grease such as illegal cooking oil can solve the problems by technical ideas and ways once and for all.
At present, two methods of alkali refining (chemical) and distillation (physical) are mainly used for treating the grease with high fatty acid content. However, the alkali refining by a chemical method or the physical deacidification directly removes free fatty acid in the grease, so that the energy consumption, the time consumption and the pollution are reduced, and the oil product loss is large; esterification is another commonly used chemical method, which not only can convert fatty acid in high-acid-value grease into ester, reduce loss and effectively avoid post-treatment of the fatty acid, etc. However, the existing esterification process is more traditional, and after-treatment is needed when a catalyst is used; even if the temperature is increased, the reaction time is often 8 hours or more, and the high temperature affects the product quality.
Disclosure of Invention
The invention relates to a synchronous deacidification process for high-acid-value grease without catalysis esterification and distillation. Firstly, the process has low requirements on raw materials, and can be suitable for various high-acid-value oils; secondly, in order to solve the key problem of difficult acid reduction of the tail sound of the reaction, a two-in-one process which can synchronously realize esterification removal and distillation removal of fatty acid is provided. Thereby realizing the purposes of shortening time, reducing loss, improving productivity and reducing cost.
The technical scheme of the invention is as follows: a high acid value grease non-catalytic esterification and distillation synchronous deacidification process adopts high acid value grease and glycerol as raw materials, the grease is filtered, dehydrated and degummed and then is put into a reaction kettle, and a proper amount of glycerol is added; stirring and heating to 200-210 ℃ under vacuum, and reacting for 30-60 minutes; then heating to 220-230 ℃, and reacting for 30-180 minutes; and finally, controlling the temperature to be 220-240 ℃, ensuring the pressure to be lower than 0.02MPa, injecting glycerol or water vapor from the bottom of the reaction kettle, distilling and deacidifying while esterifying, stopping injecting when the sampling acid value is lower than 2mgKOH/g, stopping reacting when no distillate exists basically, and cooling and discharging to obtain the fatty glyceride product with the low acid value.
The high acid value grease is various acidified oils and swill-cooked dirty oil.
The reaction kettles are used singly or in series.
The glycerin and fatty acid produced in the production process are dehydrated and then put into the reaction kettle again or directly injected into the first reaction kettle after series connection to enter a reaction system for recycling.
Has the advantages that:
the invention provides a high-acid-value grease non-catalytic esterification and distillation synchronous deacidification process for the grease chemical utilization industry; also provides a high-quality fatty glyceride raw material for the biodiesel industry. The method realizes the synchronous deacidification of the combination of the esterification deacidification and the distillation deacidification of the high-acid-value oil in the process, and can quickly and efficiently realize the aim of deacidification of the oil, thereby realizing the aims of shortening time, reducing loss, improving productivity and reducing cost.
The raw materials used in the invention are various acidified oils, high acid value grease of illegal cooking oil and glycerin; the process can synchronously realize esterification removal and distillation removal of fatty acid in the grease, and quickly realize the purpose of reducing acid value with low loss. The catalyst can be added or a plurality of kettles can be added for reaction in series according to actual needs.
The reaction in the reaction kettle is divided into 3 stages: controlling the temperature to be 200-210 ℃, carrying out vacuum dehydration reaction for 30-60 minutes, carrying out primary esterification on glycerol, and avoiding the glycerol from evaporating at a low temperature; 2. heating to 220-230 ℃, carrying out vacuum dehydration reaction for 30-180 minutes, and promoting esterification at high temperature in the main fatty acid esterification stage; 3. controlling the temperature to be 220-240 ℃, ensuring the pressure to be lower than 0.02MPa, injecting glycerin or water vapor from the bottom of the reaction kettle, performing distillation deacidification while performing esterification, strengthening deacidification stage, and performing alcohol supplement and distillation deacidification synchronously.
The invention can realize the purpose of directly preparing high-purity fatty glyceride from high-acid-value grease without improving the existing equipment, glycerin and fatty acid generated in the production process can be put into a reaction kettle again after dehydration (2), and zero loss is realized in continuous production.
Drawings
FIG. 1 is a schematic diagram of a synchronous esterification and distillation deacidification process. In the figure, a reaction kettle (1) is subjected to flash evaporation (2), a storage tank (3), a glycerin tank (4) and a grease tank (5).
Detailed Description
A synchronous deacidification process for high-acid-value grease without catalysis esterification and distillation. Adopting high-acid-value grease and glycerol as raw materials, carrying out pretreatment such as filtration, dehydration and degumming on the grease, then loading the grease into a reaction kettle, and adding a proper amount of glycerol according to the initial acid value; firstly, stirring and heating to 200-210 ℃ under vacuum, and carrying out dehydration reaction for 30-60 minutes to realize pre-esterification of glycerol (prevent a large amount of fatty acid from being carried out by distillation after heating and pressure reduction); then heating to 220-230 ℃, and carrying out dehydration reaction for 30-180 minutes to realize mass esterification of fatty acid; and finally, controlling the temperature to be 220-240 ℃, ensuring the pressure to be lower than 0.02MPa (the saturated vapor pressure of stearic acid at 173 ℃ is about 0.133kPa, and the boiling point of glycerin is reduced to be lower than 230 ℃ at the temperature of lower than 20 kPa), injecting glycerin or water vapor from the bottom of the reaction kettle, and distilling and deacidifying while esterifying (alcohol supplement can effectively improve the hydrogen ion concentration of hydroxyl dissociation to promote esterification reaction, can also ensure the content of distillable glycerin, and can reduce glycerin polymerization at high temperature and low pressure to ensure the distillation of the glycerin and the removal of fatty acid. Stopping injecting when the sampling acid value is lower than expected (such as 2mgKOH/g), stopping reaction when no distillate exists basically, and cooling and discharging to obtain the fatty glyceride product with low acid value. The method can synchronously realize esterification (chemical method) and distillation removal (physical deacidification) of fatty acid in the grease, and quickly realize the purpose of reducing acid value with low loss.
The invention can realize the purpose of directly preparing high-purity fatty glyceride from high-acid-value grease without improving the existing equipment, thereby greatly reducing the loss of fatty acid in physical decarboxylation and improving the yield; and the acid value can be effectively reduced, the reaction time is shortened, and the quality of the esterification product is improved. Glycerol and fatty acid produced in the production process can be put into the reaction kettle of the next batch again after dehydration, and zero loss is realized in continuous production.
The raw materials are various recycled high acid value oil such as drainage oil and glycerin; in addition, a catalyst can be added or a plurality of kettles can be added for reaction in series according to actual needs.
Example 1:
raw materials: gutter oil (acid value 78mgKOH/g), glycerin;
adding 100 parts (by mass, the same below) of pretreated illegal cooking oil and 12 parts of glycerol into a reaction kettle (1), starting stirring, heating to 205 ℃, and carrying out dehydration reaction for 60 minutes under the pressure of 0.07 MPa; then heating to 220 ℃, and carrying out dehydration reaction for 120 minutes; and finally, controlling the temperature at 230 ℃ and the pressure at 0.001MPa, injecting hot glycerin (110 ℃) from the bottom of the reaction kettle, and distilling and deacidifying while esterifying. The reaction was carried out for 60 minutes, and the sample was taken out and had an acid value of 1.94mgKOH/g, and the injection of glycerin was stopped, and the reaction was stopped when there was substantially no distillate. And cooling and discharging to obtain the fatty glyceride product with low acid value. All fractions are dehydrated by flash evaporation (2) and then injected into a storage tank (3) for use in the next kettle.
Example 2:
raw materials: acidified oil (acid value 148mgKOH/g), glycerin;
adding 100 parts of pretreated acidified oil and 15 parts of glycerol into a reaction kettle (1), starting stirring, heating to 210 ℃, controlling the pressure to be 0.05MPa, and performing dehydration reaction for 30 minutes; then the temperature is increased to 230 ℃, and dehydration reaction is carried out for 150 minutes; and finally, controlling the temperature at 240 ℃ and the pressure at 0.002MPa, injecting hot glycerin (110 ℃) from the bottom of the reaction kettle, and distilling and deacidifying while esterifying. Reacting for 90 minutes, sampling the fatty acid glyceride with an acid value of 1.98mgKOH/g, stopping injecting the glycerol, stopping the reaction when no distillate exists basically, and cooling and discharging to obtain the fatty acid glyceride product with a low acid value. All fractions are dehydrated by the dehydrator (2) and then injected into the storage tank (3) for use in the next kettle.
Example 3:
raw materials: gutter oil (acid value 51mgKOH/g), glycerin;
adding 100 parts of the pretreated illegal cooking oil and 11 parts of glycerol into a reaction kettle (1), starting stirring, heating to 210 ℃, controlling the pressure to be 0.03MPa, and performing dehydration reaction for 20 minutes; then the temperature is increased to 230 ℃, and dehydration reaction is carried out for 70 minutes; and finally, controlling the temperature at 235 ℃ and the pressure at 0.001MPa, injecting hot glycerin (115 ℃) from the bottom of the reaction kettle, and distilling and deacidifying while esterifying. Reacting for 30 minutes, sampling the acid value to be 1.99mgKOH/g, stopping injecting the glycerol, stopping reacting when no distillate exists basically, and cooling and discharging to obtain the fatty glyceride product with the low acid value. All fractions are dehydrated by a distillation kettle (2) and then injected into a storage tank (3) for the next kettle.
Example 4:
raw materials: acidified oil and fat (acid value: 106mgKOH/g), glycerin;
adding 100 parts of pretreated acidified oil and 13 parts of glycerol into a reaction kettle (1), starting stirring, heating to 210 ℃, controlling the pressure to be 0.04MPa, and performing dehydration reaction for 60 minutes; then heating to 220 ℃, and carrying out dehydration reaction for 200 minutes; and finally, controlling the temperature at 225 ℃, adjusting the pressure to 0.001MPa, injecting steam from the bottom of the reaction kettle, and distilling and deacidifying while esterifying. Reacting for 60 minutes, sampling the fatty acid glyceride with an acid value of 1.93mgKOH/g, stopping injecting steam, stopping reacting when no distillate exists basically, and cooling and discharging to obtain the fatty acid glyceride product with a low acid value. All fractions are dehydrated by a distillation kettle (2) and then injected into a storage tank (3) for the next kettle.
The examples are only for describing the implementation method, and any change of the raw material ratio, the reaction temperature, the addition of the catalyst or the serial connection of a plurality of reaction kettles by the conventional means in the field (which is convenient for continuous production) still falls into the protection scope of the patent by adopting the principle of the method.
Claims (4)
1. A high acid value grease non-catalytic esterification and distillation synchronous deacidification process is characterized in that: adopting high-acid-value grease and glycerol as raw materials, filtering, dehydrating and degumming the grease, then putting the pretreated grease into a reaction kettle, and adding a proper amount of glycerol; stirring and heating to 200-210 ℃ under vacuum, and reacting for 30-60 minutes; then heating to 220-230 ℃, and reacting for 30-180 minutes; and finally, controlling the temperature to be 220-240 ℃, ensuring the pressure to be lower than 0.02MPa, injecting glycerol or water vapor from the bottom of the reaction kettle, distilling and deacidifying while esterifying, stopping injecting when the sampling acid value is lower than 2mgKOH/g, stopping reacting when no distillate exists basically, and cooling and discharging to obtain the fatty glyceride product with the low acid value.
2. The non-catalytic esterification and distillation synchronous deacidification process for high acid value grease according to claim 1, wherein the high acid value grease is various acidified oils and illegal cooking oils.
3. The non-catalytic esterification and distillation synchronous deacidification process for high acid value grease according to claim 1, wherein the reaction kettle is used singly or in series.
4. The non-catalytic esterification and distillation synchronous deacidification process for high acid value grease as claimed in claim 1, wherein the glycerol and fatty acid produced in the production process are dehydrated and then put into the reaction kettle again or directly injected into the first reaction kettle after series connection to enter the reaction system for recycling.
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| CN202110213057.XA CN112980488A (en) | 2021-02-25 | 2021-02-25 | High-acid-value grease non-catalytic esterification and distillation synchronous deacidification process |
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| CN202110213057.XA CN112980488A (en) | 2021-02-25 | 2021-02-25 | High-acid-value grease non-catalytic esterification and distillation synchronous deacidification process |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103013681A (en) * | 2012-12-28 | 2013-04-03 | 北京石油化工学院 | Method for preparing fatty acid methyl ester by using waste edible oil |
| CN103173293A (en) * | 2011-12-26 | 2013-06-26 | 北京石油化工学院 | Method for preparing biodiesel by utilizing high-acid value oil |
| CN105038995A (en) * | 2015-08-21 | 2015-11-11 | 中国林业科学研究院林产化学工业研究所 | Non-catalytic esterification deacidification method for high-acid-value grease |
| CN107459997A (en) * | 2017-07-21 | 2017-12-12 | 中国林业科学研究院林产化学工业研究所 | A kind of high acid value waste oil glycerine is without catalytic esterification deacidification continuous production technology |
-
2021
- 2021-02-25 CN CN202110213057.XA patent/CN112980488A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103173293A (en) * | 2011-12-26 | 2013-06-26 | 北京石油化工学院 | Method for preparing biodiesel by utilizing high-acid value oil |
| CN103013681A (en) * | 2012-12-28 | 2013-04-03 | 北京石油化工学院 | Method for preparing fatty acid methyl ester by using waste edible oil |
| CN105038995A (en) * | 2015-08-21 | 2015-11-11 | 中国林业科学研究院林产化学工业研究所 | Non-catalytic esterification deacidification method for high-acid-value grease |
| CN107459997A (en) * | 2017-07-21 | 2017-12-12 | 中国林业科学研究院林产化学工业研究所 | A kind of high acid value waste oil glycerine is without catalytic esterification deacidification continuous production technology |
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Application publication date: 20210618 |