CN111378524A - Method for processing grease by using low-concentration phosphoric acid - Google Patents
Method for processing grease by using low-concentration phosphoric acid Download PDFInfo
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- CN111378524A CN111378524A CN201811630427.4A CN201811630427A CN111378524A CN 111378524 A CN111378524 A CN 111378524A CN 201811630427 A CN201811630427 A CN 201811630427A CN 111378524 A CN111378524 A CN 111378524A
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- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 title claims abstract description 228
- 229910000147 aluminium phosphate Inorganic materials 0.000 title claims abstract description 114
- 238000000034 method Methods 0.000 title claims abstract description 61
- 239000004519 grease Substances 0.000 title claims abstract description 39
- 239000003513 alkali Substances 0.000 claims abstract description 40
- 239000003921 oil Substances 0.000 claims description 71
- 238000009874 alkali refining Methods 0.000 claims description 17
- 239000003925 fat Substances 0.000 claims description 17
- 238000007670 refining Methods 0.000 claims description 10
- 239000003518 caustics Substances 0.000 claims description 4
- 238000003672 processing method Methods 0.000 claims description 3
- 150000003904 phospholipids Chemical class 0.000 abstract description 33
- 230000008569 process Effects 0.000 abstract description 31
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- 239000000243 solution Substances 0.000 description 63
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- 239000002253 acid Substances 0.000 description 21
- 235000011121 sodium hydroxide Nutrition 0.000 description 20
- 239000010779 crude oil Substances 0.000 description 16
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 13
- 239000000203 mixture Substances 0.000 description 12
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- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 4
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- 239000011574 phosphorus Substances 0.000 description 4
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- 230000009286 beneficial effect Effects 0.000 description 3
- 238000005119 centrifugation Methods 0.000 description 3
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 230000003472 neutralizing effect Effects 0.000 description 3
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- 150000007525 superbases Chemical class 0.000 description 2
- 235000019871 vegetable fat Nutrition 0.000 description 2
- 239000008158 vegetable oil Substances 0.000 description 2
- PORPENFLTBBHSG-MGBGTMOVSA-N 1,2-dihexadecanoyl-sn-glycerol-3-phosphate Chemical compound CCCCCCCCCCCCCCCC(=O)OC[C@H](COP(O)(O)=O)OC(=O)CCCCCCCCCCCCCCC PORPENFLTBBHSG-MGBGTMOVSA-N 0.000 description 1
- 235000019489 Almond oil Nutrition 0.000 description 1
- 235000007542 Cichorium intybus Nutrition 0.000 description 1
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- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 1
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Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B3/00—Refining fats or fatty oils
- C11B3/02—Refining fats or fatty oils by chemical reaction
- C11B3/04—Refining fats or fatty oils by chemical reaction with acids
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Microbiology (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Wood Science & Technology (AREA)
- Organic Chemistry (AREA)
- Fats And Perfumes (AREA)
Abstract
The invention discloses a method for processing grease, which comprises the step of degumming the grease by using a phosphoric acid solution with the concentration of 30-60 wt%. According to the invention, the concentration of the phosphoric acid solution used in the oil degumming process is reduced, and the volume of the phosphoric acid solution is increased, so that the mixing contact area of phosphoric acid and an oil product is increased, the mixing efficiency is finally increased, and the function of chelating non-hydrated phospholipid by phosphoric acid is fully exerted. The method of the invention reduces the phospholipid content of the chemically refined grease, simultaneously reduces the consumption of phosphoric acid and alkali liquor auxiliary materials, finally reduces the loss of oil products caused by chemical reaction, and improves the product yield.
Description
Technical Field
The invention belongs to the field of grease processing, and particularly relates to a method for removing phospholipid in grease.
Background
In the grease processing process, impurities in crude oil are generally required to be removed through a chemical refining process. Phospholipids, which are common impurities in crude oil, can be classified into hydrated phospholipids and non-hydrated phospholipids. The phospholipids contained in the crude oil deteriorate the flavor and stability of the oil and fat product, and cause foaming of the oil and fat during use.
The process of removing phospholipids from fats and oils is called degumming. The hydrated phospholipid can be removed by adding a proper amount of water into the crude oil, and then removing the hydrated phospholipid by sedimentation or centrifugation. However, non-hydrated phospholipids produced by under-ripening, deterioration and processing of oil are insoluble in water, and some processing aids are required to convert the non-hydrated phospholipids into hydrated phospholipids for removal. The common degumming method is to add a certain amount of phosphoric acid and water into the crude oil and then stir and separate the mixture. The phosphoric acid can change the structure of the non-hydrated phospholipid to convert the non-hydrated phospholipid into the oil-insoluble phosphatidic acid state. After the crude oil is degummed by phosphoric acid, a certain amount of alkali liquor is required to be added into the oil, and the pH value of the alkali liquor is regulated to be neutral, so that the neutralized oil is obtained. In the acid and alkali treatment process, a small amount of grease can generate chemical reaction, grease loss is caused, and the product yield is reduced.
In the conventional phospholipid removal process at present, the concentration of a commonly used phosphoric acid solution is 75-85 wt%. Because of the different phospholipid contents of the different crude oils, the consumption of phosphoric acid solution (calculated by the mass percentage of the phosphoric acid solution with the consumption concentration of 85 wt% of crude oil per unit mass) is different corresponding to the processing of different crude oils: high phosphorus soybean oil (phospholipid content greater than 600ppm) about 0.05%, degummed soybean oil (phospholipid content less than 150ppm) about 0.03%, degummed rape oil (phospholipid content less than 150ppm) about 0.05%, and crude corn oil (phospholipid content greater than 400ppm) about 0.05%; the dosage of the processing excess alkali liquor is generally controlled to be 20-30% of the theoretical alkali dosage. The consumption of phosphoric acid and lye needs to be reduced.
Therefore, there is a need in the art for a method of processing fats and oils that can reduce the consumption of phosphoric acid and alkali solution in degumming and alkali refining processes, and increase the yield of the products.
Disclosure of Invention
In order to solve the problems, the invention improves the volume of the phosphoric acid solution by reducing the concentration of the phosphoric acid solution used in the oil degumming process, thereby improving the mixing contact area of phosphoric acid and oil products, finally improving the mixing efficiency and fully playing the role of chelating non-hydrated phospholipid by phosphoric acid. The method of the invention reduces the phospholipid content of the chemically refined grease, simultaneously reduces the consumption of phosphoric acid and alkali liquor auxiliary materials, finally reduces the loss of oil products caused by chemical reaction, and improves the product yield.
The invention provides a grease degumming method which comprises the step of degumming grease by using a phosphoric acid solution with the concentration of 30-60 wt%.
In one or more embodiments, the volume ratio of the grease to the phosphoric acid solution is (500-5000): 1.
in one or more embodiments, the concentration of the phosphoric acid solution is 30 to 50% by weight.
In one or more embodiments, the concentration of the phosphoric acid solution is 30 to 40% by weight.
In one or more embodiments, the volume ratio of the grease to the phosphoric acid solution is (1000-5000): 1.
in one or more embodiments, the amount of phosphoric acid used per unit mass of degumming is 0.7kg/t or less, preferably 0.5kg/t or less, and more preferably 0.4kg/t or less.
The invention also provides a grease processing method, which comprises a degumming step and an alkali refining step, wherein the degumming step uses a phosphoric acid solution with the concentration of 30-60 wt% to carry out degumming on the grease.
In one or more embodiments, the volume ratio of the grease to the phosphoric acid solution is (500-5000): 1.
in one or more embodiments, the concentration of the phosphoric acid solution is 30 to 50% by weight.
In one or more embodiments, the concentration of the phosphoric acid solution is 30 to 40% by weight.
In one or more embodiments, the volume ratio of the grease to the phosphoric acid solution is (1000-5000): 1.
in one or more embodiments, the amount of phosphoric acid used per unit mass of degumming is 0.7kg/t or less, preferably 0.5kg/t or less, and more preferably 0.4kg/t or less.
In one or more embodiments, the amount of overbase in the caustic refining step is within 15% of the theoretical amount of base.
The invention has the following positive effects:
1. the consumption of phosphoric acid and alkali liquor is effectively reduced, and the processing cost is reduced;
2. the loss of the grease in the processing process is reduced, and the product yield is improved;
3. the method is beneficial to the protection of national mineral resources;
4. reduces the generation of waste water and is beneficial to energy conservation and emission reduction.
Drawings
FIG. 1 is a schematic view of a grease neutralization process.
Detailed Description
The present invention will be further described with reference to the following embodiments. It should be understood that the following detailed description is illustrative of the invention only and is not intended to limit the scope of the invention.
In the present invention, all embodiments and preferred embodiments mentioned herein may be combined with each other to form a new technical solution, if not specifically stated.
In the present invention, all the technical features mentioned herein and preferred features may be combined with each other to form a new technical solution, if not specifically stated.
In the present invention, the numerical range "a to b" includes the case where the numerical value is a or b. Unless otherwise stated, the numerical range "a-b" represents a shorthand representation of any combination of real numbers between a and b, where a and b are both real numbers. For example, a numerical range of "0 to 5" means that all real numbers between "0 to 5" have been listed herein, and "0 to 5" is simply a shorthand representation of the combination of these values.
In the present invention, unless otherwise specified, "combinations thereof" mean multicomponent mixtures of the elements in question, for example two, three, four and up to the maximum possible.
In the present invention, the percentages are weight percentages (i.e., wt% or wt%), unless otherwise specified.
The inventor of the invention finds that the effect of improving the efficiency of chelating non-hydrated phospholipid by phosphoric acid can be achieved by reducing the concentration of the phosphoric acid solution for degumming the oil and increasing the volume of the phosphoric acid solution. Meanwhile, the water contained in the dilute acid plays a good role in flocculation of the hydrated phospholipid and is beneficial to the precipitation of large-particle phospholipid, so that the content of the finished oil phospholipid is reduced. The invention can reduce the consumption of phosphoric acid, thereby reducing the consumption of alkali liquor for neutralization, averagely reducing the consumption of the alkali liquor by more than 15 percent, and improving the processing yield.
Specifically, the invention provides a grease degumming method, which comprises the step of degumming grease by using a phosphoric acid solution with the concentration of 30-60 weight percent (wt%).
Fats and oils suitable for use in the present invention include various natural fats and oils and combinations thereof. The natural oil and fat can be various vegetable oil and fat and/or animal oil and fat obtained by conventional means. Examples of vegetable oils and fats suitable for use in the present invention include, but are not limited to, soybean oil (also referred to as soybean oil), rice oil, sunflower oil (also referred to as sunflower oil), palm oil, palm kernel oil, peanut oil, rapeseed oil (also referred to as rapeseed oil), cottonseed oil, safflower oil, perilla seed oil, tea seed oil, palm fruit oil, coconut oil, olive oil, cocoa butter, Chinese tallow tree seed oil, almond oil, tung seed oil, rubber seed oil, rice bran oil, corn germ oil (also referred to as corn oil), wheat germ oil, sesame seed oil, castor bean oil, linseed oil, evening primrose seed oil, hazelnut oil, walnut oil, grape seed oil, sesame seed oil, glass chicory seed oil, sea buckthorn seed oil, tomato seed oil, pumpkin seed oil, macadamia nut oil, cocoa butter, algae oil, and the like. Examples of animal fats and oils suitable for use in the present invention include, but are not limited to, beef tallow, lard, mutton fat, chicken fat, fish oil, seal oil, whale oil, dolphin oil, oyster oil, and the like.
Herein, phosphoric acid solution means phosphoric acid (H)3PO4) An aqueous solution of (a). The concentration of the phosphoric acid solution means the weight percentage (wt%) of phosphoric acid to the aqueous solution of phosphoric acid.
In the present invention, degumming may be performed by conventional degumming methods known to those skilled in the art, such as but not limited to methods in Bailey oil chemistry and technology (vol. sixth). In certain embodiments of the invention, degumming comprises: adding acid solution into oil, stirring, heating, performing solid-liquid separation, and collecting liquid phase. The degumming temperature can be 70-100 ℃, and preferably 70-90 ℃. The degumming time can be 30 minutes to 5 hours, preferably 1 to 3 hours. The solid-liquid separation can be centrifugal separation or filtration separation and the like.
In certain embodiments, the present invention uses a high shear mixer to agitate and mix the phosphoric acid solution and the grease to increase the mixing efficiency of the phosphoric acid solution and the grease.
In certain embodiments, the concentration of the phosphoric acid solution used in the present invention is 30 to 50% by weight, such as 35 to 50% by weight or 30 to 40% by weight or 35 to 40% by weight.
In some embodiments, the volume ratio of the grease to the phosphoric acid solution is (500-5000): 1, preferably (1000 to 5000): 1.
in certain embodiments, the amount of phosphoric acid used (i.e., the amount of acid added) per unit mass of degummed oil is less than or equal to 0.7kg/t, such as less than or equal to 0.6kg/t, preferably less than or equal to 0.5kg/t, more preferably less than or equal to 0.4kg/t, and can be, for example, between 0.01 and 0.7 kg/t.
As used herein, the amount of acid added refers to phosphoric acid (H) in phosphoric acid solutions of different concentrations practically used in degumming of fat and oil per unit mass3PO4) The amount of the compound can be adjusted according to the sum of the contents of the hydrated phospholipid and the non-hydrated phospholipid in the crude oil. Wherein, the detection of the content of the hydrated phospholipid refers to GB 5009.87-2016; the content of non-hydrated phospholipid is detected in the literature "Myrica rubra et al, non-hydrated phospholipid and its quantitative determination", J.China health test, 2008, Vol.18, No. 1, pp.71 and 154 ".
The invention also provides a grease processing method, which comprises a degumming step and an alkali refining step, wherein the degumming step comprises degumming the grease by using a phosphoric acid solution with the concentration of 30-60 wt%.
In certain embodiments, the concentration of the phosphoric acid solution used in the present invention is 30 to 50% by weight, such as 35 to 50% by weight or 30 to 40% by weight or 35 to 40% by weight.
In some embodiments, the volume ratio of the grease to the phosphoric acid solution is (500-5000): 1, preferably (1000 to 5000): 1.
in certain embodiments, the acid is added in an amount of 0.7kg/t or less, such as 0.6kg/t or less, preferably 0.5kg/t or less, more preferably 0.4kg/t or less, for example between 0.15 and 0.7kg/t, during the degumming step.
In the present invention, the alkali refining step can be performed by a conventional alkali refining method known to those skilled in the art, such as, but not limited to, the method in Belley oil chemistry and technology (vol. sixth). In certain embodiments of the invention, the caustic refining step comprises: adding alkali liquor into the grease for reaction, adding hot water for washing to remove soap, and drying. The alkali refining temperature can be normal temperature to 90 ℃, and is preferably 40 ℃ to 50 ℃. The alkali refining time can be 5 to 60 minutes, preferably 5 to 20 minutes.
The lye may be any alkaline solution, preferably sodium hydroxide solution and/or potassium hydroxide solution. The lye concentration is usually not more than 70% by weight, and may be, for example, 50% by weight.
Herein, the alkali addition amount is the amount of the sodium hydroxide solution actually used in the oil alkali refining of unit mass, and the calculation formula is as follows:
the addition of alkali was 0.142 FFA (1+ excess alkali) 1000/W
Wherein: FFA is the content of free fatty acid in the grease, and the unit is wt%;
w is the mass percentage concentration of the sodium hydroxide solution, and the unit is wt%;
the unit of the alkali addition amount is kg/t.
Herein, the theoretical alkali amount refers to the theoretical amount of alkali liquor required for neutralizing acidic substances inherent in the grease in the alkali refining step; the excess alkali amount refers to the ratio of the difference value between the actual dosage and the theoretical dosage of the alkali liquor used for neutralizing the grease and the theoretical dosage to the actual dosage in the actual production process.
In certain embodiments, the amount of overbase in the caustic refining step is within 15% of the theoretical amount of base (15% overbase), preferably within 10% (10% overbase).
The soapstock may be separated by conventional means. For example, the oil soap is separated by centrifugation. In certain embodiments, deionized water at a temperature of 70-95 deg.C, 10-20% by weight of the oil, may be added and stirred for 10 minutes, followed by centrifugation of the soapstock. In some embodiments, after the soaping, hot water with the weight of 5-10% of that of oil can be added, and optionally a proper amount of citric acid can be added, further water washing is carried out for 10-30 minutes, and then centrifugal dehydration, drying and gas evolution are carried out.
Herein, the calculation formula of the actual yield of the neutralized oil is as follows:
actual yield is 100% of oil mass produced/crude oil mass.
FIG. 1 shows a schematic diagram of a grease neutralization process, which generally comprises the steps of adding acid, adding alkali, heating, removing soap and the like. As shown in FIG. 1, dilute phosphoric acid with a concentration of 30-60% is used in the acid addition reaction stage of the present invention.
The invention will be described below by way of examples. It should be understood that these examples are illustrative only and are not intended to limit the scope of the present invention. The methods, reagents and conditions employed in the examples are, unless otherwise indicated, those conventional in the art.
Example 1: chemical refining of corn oil
Firstly, heating crude corn oil to 75 ℃, adding phosphoric acid solutions with different concentrations, wherein the adding amount of the phosphoric acid solution is 0.02-0.1 vol%, and adding liquid caustic soda (NaOH solution) with the concentration of 50 wt% after reacting for 2.5 hours. In the case of using 35 wt% or 50 wt% phosphoric acid solution, the amount of the superbase is 10%; in the case of using 85 wt% phosphoric acid solution, the amount of the overbase was 30%. And (3) after 10 minutes of alkali reaction, adding the mixture into a soapstock removal centrifugal machine to separate soapstock, adding hot water with the weight of 5-8% of oil into the separated soapstock removal oil, washing for 15 minutes, adding the mixture into a dehydration centrifugal machine to separate and dehydrate, heating to 95-100 ℃ after dehydration, adding the mixture into a vacuum drying tower, further dehydrating, and cooling to 40 ℃ to produce neutralized oil.
Table 1 shows the acid addition and alkali addition for degumming and alkali refining of crude corn oil (samples 1-1, 1-2 and 1-3) with different concentrations of phosphoric acid, and the product yield.
Table 1: acid adding amount and alkali adding amount of corn oil and yield of neutralized oil
| Sample No. 1-1 | Samples 1 to 2 | Samples 1 to 3 | |
| Crude oil FFA (wt%)/containing phosphorus (ppm) | 2.38/381 | 2.268/459 | 2.79/322 |
| Phosphoric acid concentration (wt%) | 35 | 50 | 85 |
| Amount of acid added (kg/t) | 0.187 | 0.17 | 0.816 |
| Amount of phosphoric acid solution (L/t) | 0.44 | 0.26 | 0.57 |
| Amount of alkali added (kg/t) | 7.44 | 7.09 | 10.3 |
| Actual yield of neutralized oil (%) | 92.3 | 93.1 | 90.5 |
As can be seen from Table 1, the acid addition and alkali addition for degumming and alkali refining of crude corn oil by the method of the present invention are lower than those for the 85 wt% phosphoric acid solution used in the degumming step; the actual yield of corn oil neutralized oil produced by the process of the present invention is higher than the yield of neutralized oil produced by using a 85 wt.% phosphoric acid solution in the degumming step.
The corn oil was continuously processed in the factory for 9 months by using a 35 wt% phosphoric acid process and a 85 wt% phosphoric acid process, respectively. As can be seen from the results of the runs for treating corn oil using the two processes shown in Table 2, the average reduction in lye consumption was 26.56% for the 35 wt.% phosphoric acid process versus the 85 wt.% phosphoric acid process.
Table 2: corn oil neutralization oil yield and liquid caustic soda consumption of 9 months of operation
| Process for preparing 35 wt% concentration phosphoric acid | 85 wt% concentration phosphoric acid process | |
| Average yield of neutralized oil | 93.37％ | 91.79％ |
| Consumption per unit of liquid caustic soda (kg/t) | 9.18 | 12.5 |
Example 2: chemical refining of soybean oil
Firstly, heating soybean oil crude oil to 75 ℃, adding phosphoric acid solutions with different concentrations, wherein the addition amount of the phosphoric acid solution is 0.02-0.1 vol%, and after reacting for 2.5 hours, adding liquid alkali (NaOH solution) with the concentration of 50 wt%. In the case of using a 35 wt% phosphoric acid solution, the amount of the superbase was 5%; in the case of using 85 wt% phosphoric acid solution, the amount of the overbase was 30%. And (3) after 10 minutes of alkali reaction, adding the mixture into a soapstock removal centrifugal machine to separate soapstock, adding hot water with the weight of 5-8% of oil into the separated soapstock removal oil, washing for 15 minutes, adding the mixture into a dehydration centrifugal machine to separate and dehydrate, heating to 95-100 ℃ after dehydration, adding the mixture into a vacuum drying tower, further dehydrating, and cooling to 40 ℃ to produce neutralized oil.
Table 3 shows the acid addition and alkali addition for degumming and alkali refining of crude soybean oil (samples 2-1, 2-2 and 2-3) with different concentrations of phosphoric acid, and the product yield.
Table 3: acid adding amount and alkali adding amount of soybean oil and yield of neutralized oil
| Sample No. 2-1 | Sample No. 2-2 | Samples 2 to 3 | |
| Crude oil FFA (wt%)/containing phosphorus (ppm) | 0.51/147 | 0.81/143 | 1/222 |
| Phosphoric acid concentration (wt%) | 35 | 35 | 85 |
| Amount of acid added (kg/t) | 0.247 | 0.366 | 0.689 |
| Amount of phosphoric acid solution (L/t) | 0.77 | 1.14 | 0.48 |
| Amount of alkali added (kg/t) | 1.52 | 2.42 | 3.69 |
| Actual yield of neutralized oil (%) | 98.1 | 97.95 | 96.81 |
As can be seen from table 3, the amount of acid and alkali used for degumming and alkali refining of soybean oil crude oil by the method of the present invention was lower than that used for using a phosphoric acid solution having a concentration of 85 wt% in the degumming step; the actual yield of the soybean oil neutralized oil prepared by the process of the present invention is higher than the yield of the neutralized oil obtained by using a phosphoric acid solution having a concentration of 85% by weight in the degumming step.
Soybean oil was continuously treated in the factory for 9 months by using a 35 wt% phosphoric acid process and a 85 wt% phosphoric acid process, respectively. From the results of the runs for treating soybean oil with the two processes given in table 4, it can be seen that the average reduction in lye consumption was 19.95% with the 35 wt% phosphoric acid process compared to the 85 wt% phosphoric acid process.
Table 4: soybean oil neutralizing oil yield and liquid caustic soda consumption of 9 months of operation
| Process for preparing 35 wt% concentration phosphoric acid | 85 wt% concentration phosphoric acid process | |
| Average yield of neutralized oil | 97.74％ | 96.81％ |
| Consumption per unit of liquid caustic soda (kg/t) | 3.13 | 3.91 |
Example 3: degumming and alkali refining of rape oil
Firstly, heating crude rape oil to 75 ℃, adding phosphoric acid solutions with different concentrations, wherein the adding amount of the phosphoric acid solution is 0.02-0.1 vol%, and adding liquid alkali (NaOH solution) with the concentration of 50 wt% after reacting for 2.5 hours. In the case of using 35 wt% or 50 wt% phosphoric acid solution, the amount of the overbase was 8%; in the case of using 85 wt% phosphoric acid solution, the amount of the overbase was 30%. And (3) after 10 minutes of alkali reaction, adding the mixture into a soapstock removal centrifugal machine to separate soapstock, adding hot water with the weight of 5-8% of oil into the separated soapstock removal oil, washing for 15 minutes, adding the mixture into a dehydration centrifugal machine to separate and dehydrate, heating to 95-100 ℃ after dehydration, adding the mixture into a vacuum drying tower, further dehydrating, and cooling to 40 ℃ to produce neutralized oil.
Table 5 shows the acid addition and alkali addition for degumming and refining of crude rapeseed oil (samples 3-1, 3-2 and 3-3) with different concentrations of phosphoric acid, and the product yield.
Table 5: acid adding amount and alkali adding amount of rape oil and yield of neutralized oil
| Sample No. 3-1 | Sample No. 3-2 | Samples 3 to 3 | |
| Crude oil FFA (wt%)/containing phosphorus (ppm) | 0.52/244.61 | 0.67/31.8 | 0.88/182 |
| Phosphoric acid concentration (wt%) | 35 | 50 | 85 |
| Amount of acid added (kg/t) | 0.357 | 0.06 | 0.723 |
| Amount of phosphoric acid solution (L/t) | 0.84 | 0.09 | 0.50 |
| Amount of alkali added (kg/t) | 1.59 | 2.06 | 3.25 |
| Yield of neutralized oil (%) | 97.9 | 97.4 | 97.2 |
As can be seen from Table 5, the amount of acid and alkali used for degumming and alkali refining of crude rapeseed oil by the method of the present invention was lower than that used for the 85 wt% phosphoric acid solution used in the degumming step; the actual yield of the rape oil neutralized oil obtained by the method of the present invention is higher than the yield of the neutralized oil obtained by using the phosphoric acid solution with the concentration of 85 wt% in the degumming step.
Rapeseed oil was continuously treated in the plant for 9 months by using a 35 wt.% phosphoric acid process and by using a 85 wt.% phosphoric acid process, respectively. As can be seen from the results of the two processes for treating rapeseed oil given in Table 6, the average reduction in consumption of lye was 22.62% in the process using phosphoric acid at a concentration of 35% by weight compared to the process using phosphoric acid at a concentration of 85% by weight.
Table 6: the yield of the rape oil neutralization oil and the consumption of liquid caustic soda are 9 months after operation
| Process for preparing 35 wt% concentration phosphoric acid | 85 wt% concentration phosphoric acid process | |
| Average yield of neutralized oil | 97.70％ | 97.64％ |
| Consumption per unit of liquid caustic soda (kg/t) | 3.25 | 4.20 |
Comparative example 1
Chemical refining of corn oil was conducted in the same manner as in example 1, except that the 85% by weight phosphoric acid solution was added to the oil or fat, then water was added so that the phosphoric acid concentration was 35% by weight based on the total weight of the phosphoric acid solution and water added, and then degumming and alkali refining were conducted to obtain a neutral oil.
The results show that the consumption of phosphoric acid and lye is not reduced, and that the centrifugal separation burden in the subsequent separation steps is increased, the separation effect is poor, and finally the yield of neutral oil is reduced.
Comparative example 2
Chemical refining of corn oil was performed as in example 1 except that the amount of 85% strength phosphoric acid solution was reduced to 20% (i.e., the amount of acid added was 0.016% by weight of the oil).
The results show that the phospholipid content of the obtained neutralized oil is very high, and is 30% higher than that of the neutral oil treated by the phosphoric acid solution with the same weight concentration of 40%.
The above description is only a preferred embodiment of the present invention, and not intended to limit the scope of the present invention, which is defined broadly in the claims, and any other technical entity or method implemented by others, if it is exactly the same as or equivalent to the definition of the claims, will be considered to be covered by the claims.
All documents referred to herein are incorporated by reference into this application as if each were individually incorporated by reference. Furthermore, it should be understood that various changes and modifications can be made by one skilled in the art after reading the above disclosure, and equivalents may fall within the scope of the invention as defined by the appended claims.
Claims (10)
1. The oil degumming method is characterized by comprising the step of degumming the oil by using a phosphoric acid solution with the concentration of 30-60 wt%, preferably 30-50 wt%.
2. The method according to claim 1, wherein the volume ratio of the grease to the phosphoric acid solution is (500-5000): 1, preferably (1000 to 5000): 1.
3. the method according to claim 1 or 2, wherein the concentration of the phosphoric acid solution is 30 to 40% by weight.
4. A method according to any of claims 1 to 3, wherein the amount of phosphoric acid used per unit mass of degumming of fats & oils is less than or equal to 0.7kg/t, preferably less than or equal to 0.5kg/t, more preferably less than or equal to 0.4 kg/t.
5. A grease processing method comprises a degumming step and an alkali refining step, wherein the degumming step comprises degumming of grease by using a phosphoric acid solution with the concentration of 30-60 wt%, preferably 30-50 wt%.
6. The method according to claim 5, wherein the volume ratio of the grease to the phosphoric acid solution is (500-5000): 1, preferably (1000 to 5000): 1.
7. the method according to claim 5 or 6, wherein the concentration of the phosphoric acid solution is 30 to 40% by weight.
8. A method according to claim 7, wherein the amount of phosphoric acid used per unit mass of degummed fat is less than or equal to 0.7kg/t, preferably less than or equal to 0.5kg/t, more preferably less than or equal to 0.4 kg/t.
9. The method of any one of claims 5 to 8, wherein in the caustic refining step, the amount of excess alkali is within 15% of the theoretical amount of alkali.
10. A grease product produced by the method of any one of claims 1 to 9.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4698185A (en) * | 1985-03-18 | 1987-10-06 | Safinco Coordination Center N.V. | Process for producing degummed vegetable oils and gums of high phosphatidic acid content |
| CN1523094A (en) * | 2003-09-12 | 2004-08-25 | 高元财 | Process for producing corn germ oil and table oil made by products produced thereby |
| CN104263509A (en) * | 2014-08-21 | 2015-01-07 | 青岛海智源生命科技有限公司 | DHA micro-algal oil degumming method |
| CN108841443A (en) * | 2018-06-26 | 2018-11-20 | 安徽谷天下食品有限公司 | A kind of refined rice bran oil combination degumming alkali refining method |
-
2018
- 2018-12-29 CN CN201811630427.4A patent/CN111378524A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4698185A (en) * | 1985-03-18 | 1987-10-06 | Safinco Coordination Center N.V. | Process for producing degummed vegetable oils and gums of high phosphatidic acid content |
| CN1523094A (en) * | 2003-09-12 | 2004-08-25 | 高元财 | Process for producing corn germ oil and table oil made by products produced thereby |
| CN104263509A (en) * | 2014-08-21 | 2015-01-07 | 青岛海智源生命科技有限公司 | DHA micro-algal oil degumming method |
| CN108841443A (en) * | 2018-06-26 | 2018-11-20 | 安徽谷天下食品有限公司 | A kind of refined rice bran oil combination degumming alkali refining method |
Non-Patent Citations (1)
| Title |
|---|
| 范兴龙: "物理精炼中脱胶工艺的探讨", no. 01, pages 31 - 32 * |
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