CN113234541A - Production process for extracting neutral oil from tank bottom material - Google Patents
Production process for extracting neutral oil from tank bottom material Download PDFInfo
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- CN113234541A CN113234541A CN202110540333.3A CN202110540333A CN113234541A CN 113234541 A CN113234541 A CN 113234541A CN 202110540333 A CN202110540333 A CN 202110540333A CN 113234541 A CN113234541 A CN 113234541A
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- 230000007935 neutral effect Effects 0.000 title claims abstract description 78
- 239000000463 material Substances 0.000 title claims abstract description 50
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 23
- 239000002253 acid Substances 0.000 claims abstract description 39
- 239000012266 salt solution Substances 0.000 claims abstract description 36
- 238000000034 method Methods 0.000 claims abstract description 29
- 238000002156 mixing Methods 0.000 claims abstract description 15
- 239000007788 liquid Substances 0.000 claims abstract description 5
- 238000003756 stirring Methods 0.000 claims description 68
- 239000000243 solution Substances 0.000 claims description 33
- 239000002585 base Substances 0.000 claims description 30
- 239000011259 mixed solution Substances 0.000 claims description 20
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 claims description 12
- TYJJADVDDVDEDZ-UHFFFAOYSA-M potassium hydrogencarbonate Chemical compound [K+].OC([O-])=O TYJJADVDDVDEDZ-UHFFFAOYSA-M 0.000 claims description 8
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 claims description 6
- 235000010265 sodium sulphite Nutrition 0.000 claims description 6
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 claims description 5
- 235000015497 potassium bicarbonate Nutrition 0.000 claims description 5
- 229910000028 potassium bicarbonate Inorganic materials 0.000 claims description 5
- 239000011736 potassium bicarbonate Substances 0.000 claims description 5
- 235000017281 sodium acetate Nutrition 0.000 claims description 5
- 239000001632 sodium acetate Substances 0.000 claims description 5
- 239000003513 alkali Substances 0.000 claims description 3
- 229910000027 potassium carbonate Inorganic materials 0.000 claims description 3
- 235000011181 potassium carbonates Nutrition 0.000 claims description 3
- UIIMBOGNXHQVGW-DEQYMQKBSA-M Sodium bicarbonate-14C Chemical compound [Na+].O[14C]([O-])=O UIIMBOGNXHQVGW-DEQYMQKBSA-M 0.000 claims description 2
- 150000008043 acidic salts Chemical class 0.000 claims 2
- 239000003921 oil Substances 0.000 abstract description 77
- 238000000605 extraction Methods 0.000 abstract description 33
- 239000010779 crude oil Substances 0.000 abstract description 9
- 235000019198 oils Nutrition 0.000 description 73
- 230000000052 comparative effect Effects 0.000 description 27
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 18
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 9
- 235000017557 sodium bicarbonate Nutrition 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 238000005119 centrifugation Methods 0.000 description 7
- 238000005303 weighing Methods 0.000 description 5
- 238000001514 detection method Methods 0.000 description 4
- 150000003839 salts Chemical class 0.000 description 4
- 235000015112 vegetable and seed oil Nutrition 0.000 description 4
- 239000008158 vegetable oil Substances 0.000 description 4
- 239000012535 impurity Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000006467 substitution reaction Methods 0.000 description 3
- 238000011282 treatment Methods 0.000 description 3
- GVJHHUAWPYXKBD-UHFFFAOYSA-N (±)-α-Tocopherol Chemical compound OC1=C(C)C(C)=C2OC(CCCC(C)CCCC(C)CCCC(C)C)(C)CCC2=C1C GVJHHUAWPYXKBD-UHFFFAOYSA-N 0.000 description 2
- 239000000084 colloidal system Substances 0.000 description 2
- 238000004132 cross linking Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000000049 pigment Substances 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 102000004169 proteins and genes Human genes 0.000 description 2
- 108090000623 proteins and genes Proteins 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 229920002472 Starch Polymers 0.000 description 1
- 229930003427 Vitamin E Natural products 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000004332 deodorization Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000003925 fat Substances 0.000 description 1
- 235000021588 free fatty acids Nutrition 0.000 description 1
- WIGCFUFOHFEKBI-UHFFFAOYSA-N gamma-tocopherol Natural products CC(C)CCCC(C)CCCC(C)CCCC1CCC2C(C)C(O)C(C)C(C)C2O1 WIGCFUFOHFEKBI-UHFFFAOYSA-N 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 150000002978 peroxides Chemical class 0.000 description 1
- 150000003904 phospholipids Chemical class 0.000 description 1
- 238000010561 standard procedure Methods 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 229940046009 vitamin E Drugs 0.000 description 1
- 235000019165 vitamin E Nutrition 0.000 description 1
- 239000011709 vitamin E Substances 0.000 description 1
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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
- C11B13/00—Recovery of fats, fatty oils or fatty acids from waste materials
-
- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/74—Recovery of fats, fatty oils, fatty acids or other fatty substances, e.g. lanolin or waxes
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- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Wood Science & Technology (AREA)
- Organic Chemistry (AREA)
- Fats And Perfumes (AREA)
- Extraction Or Liquid Replacement (AREA)
Abstract
The invention provides a production process for extracting neutral oil from tank bottoms, which mainly comprises the following steps: preparing strong base weak acid salt solution with mass concentration of 0.25-0.5%; adding strong base weak acid salt solution into the tank bottom material, wherein the volume weight (ml/g) ratio of the strong base weak acid salt solution to the tank bottom material is 10-15:100, uniformly mixing, controlling the temperature to be 25-35 ℃ to obtain mixed liquid, and centrifuging the mixed liquid to obtain neutral oil. In the process, the type and the addition amount of the strong base and weak acid salt solution are strictly controlled, so that the tank bottom material forms dispersed liquid, the extraction rate of neutral oil is favorably improved, and in addition, the obtained neutral oil product is good and can be directly used as crude oil.
Description
Technical Field
The invention relates to the technical field of raw oil tank bottom material utilization, in particular to a production process for extracting neutral oil from tank bottom material.
Background
The crude oil tank bottom material is waste solid generated when crude oil is kept still in an oil storage tank, and the waste solid contains 60-70% of neutral oil, about 10% of starch, free fatty acid, phospholipid, colloid, particle impurities, pigment, protein, crude fiber and other substances; due to the existence of the substances, the viscosity of the tank bottom materials is large and the tank bottom materials are not easy to disperse, so that the utilization rate of the tank bottom materials is low, and the tank bottom materials are wasted.
The neutral oil is an oil which can be used as crude oil after being processed, the extraction condition of the neutral oil in the tank bottom material influences the extraction rate of the vegetable oil, and in addition, the quality of the neutral oil extracted from the tank bottom material influences the quality of the vegetable oil.
The materials in the pot bottom materials are rich in variety and content, so the materials inevitably enter the neutral oil along with the extraction process in the extraction process, the extracted neutral oil can be used as the vegetable oil only by deacidification, decoloration, deodorization and other treatments, the extraction process of the neutral oil is complicated, the cost is increased, and the extraction of the neutral oil is further limited.
Therefore, the production process which is simple in process and can directly serve as crude oil to be applied to production is provided, and the method has important significance for extracting the neutral oil from the tank bottom materials.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a production process for extracting neutral oil from tank bottom materials, wherein in the process, the type and the addition amount of strong base and weak acid salt solution are strictly controlled, so that the tank bottom materials form dispersed liquid, the extraction rate of the neutral oil is favorably improved, and in addition, the obtained neutral oil is good in quality and can be directly used as crude oil.
The technical scheme of the invention is as follows:
a production process for extracting neutral oil from tank bottoms mainly comprises the following steps: preparing strong base weak acid salt solution with mass concentration of 0.25-0.5%; taking a pot bottom material, adding a strong base weak acid salt solution into the pot bottom material, wherein the volume-weight (ml/g) ratio of the strong base weak acid salt solution to the pot bottom material is 10-15:100, uniformly mixing to obtain a mixed solution, and centrifuging the mixed solution to obtain neutral oil; wherein, in the process of uniformly mixing, the temperature is controlled to be 25-35 ℃.
The neutral oil obtained by the production process has an acid value of 6.13-6.98mg/g and an extraction rate of more than 80%.
Preferably, the strong base weak acid salt solution is one of sodium bicarbonate, sodium acetate, sodium sulfite, potassium bicarbonate and potassium carbonate.
Preferably, the mass concentration of the strong base weak acid salt solution is 0.42%, and the volume weight (ml/g) ratio of the strong base weak acid salt solution to the tank bottom material is 12: 100.
Preferably, the temperature of the mixing is 28 ℃.
Further, the specific process of the production process is as follows:
(1) placing the tank bottom material in a stirring tank, then adding strong base weak acid salt solution according to the proportion, starting stirring, wherein the mixing and stirring speed is 30-40r/min, and controlling the temperature in the stirring tank to obtain a mixed solution;
(2) centrifuging the mixed solution at 3500r/min 2000-3500r/min for 2-3min to obtain layered solution, and collecting the upper layer solution as neutral oil.
Preferably, in the step (1), the stirring process is divided into two stages, the stirring speed of the first stage is 30-33r/min, the maintaining time is 25-35min, in the stage, a low-speed stirring mode is adopted to fully mix the tank bottom material and the strong base weak acid salt solution, and in the mixing process, the strong base weak acid salt solution breaks the cross-linking among colloid, protein, grease, pigment, crude fiber and the like, so that the mixed solution gradually becomes a clear suspension; the stirring speed of the second stage is 34-40r/min, the maintaining time is 30-40min, and in the stage, the stirring speed is increased to accelerate the precipitation of particle impurities and the like, so that the subsequent centrifugal extraction is facilitated.
Further, in the step (1), the strong base and weak acid salt solution is added in two times, the adding amount of the first time is 85-90% of the total amount of the strong base and weak acid salt solution, and the strong base and weak acid salt solution is added before the first-stage stirring; after the first stage of stirring is finished, the remaining strong base weak acid salt solution is added into the stirring tank.
Preferably, in step (2), the centrifugation conditions of the mixed solution are: centrifuging at 3000r/min for 2.5 min.
Compared with the prior art, the invention has the beneficial effects that:
1. in the production process provided by the invention, the treatment process is carried out at normal temperature, so that the process has the advantage of simple and easily-controlled process.
2. The neutral oil obtained by the production process has good oil quality, can be directly put into production and use, improves the extraction rate of the vegetable oil, and reduces the extraction cost of the neutral oil.
3. The production process provided by the invention can improve the extraction rate of the neutral oil by controlling the weight ratio of the strong alkali weak acid salt solution to the tank bottom material under the condition of effectively breaking the compound cross-linking in the tank bottom material, wherein the extraction rate is more than 80%.
Drawings
FIG. 1 is a photograph comparing the neutral oils after centrifugation of example 1 and comparative example 1.
FIG. 2 is a photograph comparing the neutral oils after centrifugation of example 1 and comparative example 2.
FIG. 3 is a photograph comparing the neutral oil extraction process of example 4 and comparative example 3.
Detailed Description
In order to make those skilled in the art better understand the technical solutions in the present invention, 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 only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the following examples and comparative examples of the present invention, the pot bottom material used contained neutral oil in an amount of 62.5%.
Example 1
A production process for extracting neutral oil from tank bottoms comprises the following steps:
(1) preparing strong base and weak acid salt solution: dissolving 4.2g of sodium bicarbonate in 995.8ml of water, and uniformly mixing to obtain a sodium bicarbonate solution with the mass concentration of 0.42% for later use;
(2) taking 1000g of tank bottom materials, putting the tank bottom materials into a stirring tank, adding 105.6ml of sodium bicarbonate solution obtained in the step (1) into the stirring tank, and carrying out first-stage stirring under the stirring conditions: stirring at 32r/min for 30 min; the remaining 14.4ml of sodium bicarbonate solution was then added thereto and a second stage of stirring was carried out under the following conditions: stirring at 38r/min for 36 min; controlling the temperature in the stirring tank to be 28 ℃ in the stirring processes of the first stage and the second stage; after stirring, obtaining a mixed solution;
(3) centrifuging the mixed solution at 3000r/min for 2.5min to obtain layered solution, collecting the upper layer solution as neutral oil, and weighing the neutral oil.
Example 2
A production process for extracting neutral oil from tank bottoms comprises the following steps:
(1) preparing strong base and weak acid salt solution: dissolving 2.5g of potassium carbonate in 997.5ml of water, and uniformly mixing to obtain a potassium carbonate solution with the mass concentration of 0.25% for later use;
(2) taking 1000g of tank bottom materials, placing the tank bottom materials into a stirring tank, then adding 85ml of the potassium carbonate solution obtained in the step (1) into the stirring tank, and carrying out first-stage stirring under the stirring conditions: stirring at 30r/min for 35 min; the remaining 15ml of potassium carbonate solution was then added thereto and second stage stirring was carried out under the following conditions: the stirring speed is 34r/min, and the stirring time is 40 min; controlling the temperature in the stirring tank to be 25 ℃ in the stirring processes of the first stage and the second stage; after stirring, obtaining a mixed solution;
(3) centrifuging the mixed solution at 2000r/min for 3min to obtain layered solution, collecting the upper layer solution as neutral oil, and weighing the neutral oil.
Example 3
A production process for extracting neutral oil from tank bottoms comprises the following steps:
(1) preparing strong base and weak acid salt solution: dissolving 5.0g of sodium sulfite in 995ml of water, and uniformly mixing to obtain a sodium sulfite solution with the mass concentration of 0.50% for later use;
(2) taking 1000g of tank bottom materials, placing the tank bottom materials into a stirring tank, then adding 135ml of the sodium sulfite solution obtained in the step (1) into the stirring tank, and carrying out first-stage stirring under the stirring conditions: stirring at 33r/min for 25 min; the remaining 15ml of sodium sulfite solution was then added thereto and a second stage of stirring was carried out under the following conditions: stirring at 40r/min for 30 min; controlling the temperature in the stirring tank to be 35 ℃ in the stirring processes of the first stage and the second stage; after stirring, obtaining a mixed solution;
(3) centrifuging the mixed solution at 3500r/min for 2min to obtain layered solution, collecting the upper layer solution as neutral oil, and weighing the neutral oil.
Example 4
A production process for extracting neutral oil from tank bottoms comprises the following steps:
(1) preparing strong base and weak acid salt solution: dissolving 4.2g of potassium bicarbonate in 995.8ml of water, and uniformly mixing to obtain a potassium bicarbonate solution with the mass concentration of 0.42% for later use;
(2) taking 1000g of pot bottom material, placing the pot bottom material into a stirring tank, then adding 120ml of the potassium bicarbonate solution obtained in the step (1) into the stirring tank, starting stirring, wherein the stirring speed is 37r/min, the stirring time is 90min, and the temperature is controlled to be 28 ℃ in the stirring process to obtain a mixed solution;
(3) centrifuging the mixed solution at 3000r/min for 2.5min to obtain layered solution, collecting the upper layer solution as neutral oil, and weighing the neutral oil.
Example 5
A production process for extracting neutral oil from tank bottoms comprises the following steps:
(1) preparing strong base and weak acid salt solution: dissolving 4.2g of sodium acetate in 995.8ml of water, and uniformly mixing to obtain a sodium acetate solution with the mass concentration of 0.42% for later use;
(2) taking 1000g of tank bottom material, placing the tank bottom material into a stirring tank, then adding 120ml of the sodium acetate solution obtained in the step (1) into the stirring tank, starting stirring, wherein the stirring speed is 37r/min, the stirring time is 90min, and the temperature is controlled to be 35 ℃ in the stirring process to obtain a mixed solution;
(3) centrifuging the mixed solution at 2000r/min for 3min to obtain layered solution, collecting the upper layer solution as neutral oil, and weighing the neutral oil.
The neutral oils obtained in examples 1 to 5 were examined for acid value according to GB2009.229, peroxide value according to GB5009.227, moisture according to GB5009.236, density according to GB/T5526, vitamin E according to GB 5009.82, and phytosterol according to GB/T25223, and the extraction rate of the neutral oils was calculated, and the examination results are shown in Table 1.
Table 1 neutral oil detection and extraction rates for examples 1-5
Note: extraction yield (%). ratio of neutral oil weight/(weight of pot bottom material x oil content of pot bottom material) × 100
It can be seen from table 1 that the extraction rate of neutral oil is above 80% by using the method of the present invention, the obtained neutral oil product meets the national standard, and can be used as crude oil, thereby avoiding the defect that the extracted neutral oil can be used after advanced treatment in the prior art.
Comparative example 1
The difference from example 1 is that in step (2), the amount of sodium bicarbonate solution added in the first stage was 79.2ml and the amount added in the second stage was 10.8 ml.
The centrifuged neutral oils of example 1 and comparative example 1 were photographed as shown in fig. 1, and in fig. 1, the left graph is the centrifugation result of example 1, and the right graph is the centrifugation result of comparative example 1. As can be seen from fig. 1, the neutral oil content in comparative example 1 was significantly lower as the amount of sodium bicarbonate solution added was reduced.
Comparative example 2
The difference from example 1 is that in step (2), the amount of sodium bicarbonate solution added in the first stage is 176ml and the amount added in the second stage is 24 ml.
The centrifuged neutral oils of example 1 and comparative example 2 were photographed as shown in fig. 2, and in fig. 2, the left graph is the centrifugation result of example 1, and the right graph is the centrifugation result of comparative example 2. As can be seen from fig. 2, the neutral oil content in comparative example 2 is almost not different from that of example 1 when the amount of sodium bicarbonate solution added is increased.
The results of testing the neutral oils of comparative example 1 and comparative example 2 according to the national standard method are shown in table 2.
TABLE 2 detection and extraction of neutral oils of comparative example 1 to comparative example 2
It can be seen from table 2 that when the amount of the strong base weak acid salt solution is too small, the extraction rate of the neutral oil is significantly reduced although the oil quality of the neutral oil is not significantly changed; when the addition amount of the strong base weak acid salt solution is increased, the extraction rate of neutral oil is not much different from that of the method, but the oil quality of the neutral oil is poor, and the method has better effect in combination with the quality and the extraction rate of the neutral oil.
Comparative example 3
The difference from the example 4 is that 119.5ml of water is added into 1000g of tank bottom materials, 0.5g of sodium bicarbonate is continuously added into the tank bottom materials after mixing, stirring is continuously carried out, the stirring speed is 37r/min, the total stirring time is 90min, and the rest is the same as the example 4; calculating the extraction rate to be 68.17%; and (4) detecting other indexes without detection due to low extraction rate.
The extraction rate of example 4 was 82.93%, and it was found by comparison that the extraction rates of comparative example 3 and example 4 were greatly different, and this phenomenon was caused because the contents of fats and oils, impurities, etc. in the pot bottoms were large and complicated, and in the case of adding water first, the substances in the pot bottoms became sticky with water, and after adding salt, they could not be well dispersed and the sticky lumps were not easily broken, resulting in a decrease in the extraction rate.
Photographs were taken of the experimental procedures of comparative example 3 and example 4, see figure 3. In fig. 3, the left image is a photograph of example 4, and the right image is a photograph of comparative example 3; as can be seen from the photograph, the solution of the present invention and the precipitation boundary are distinct, and the solution is in a clear and bright state, while the solution of comparative example 3 is in a turbid state.
Comparative example 4
The difference from example 4 is that the extraction rate of neutral oil was calculated by controlling the temperature to 45 deg.C, and the extraction rate was 62.5%, and in the case of low extraction rate, the quality test of neutral oil was not performed.
Comparative example 5
The difference from the example 1 is that the mass concentration of the strong base and the weak acid salt is 0.23%.
Comparative example 6
The difference from the example 1 is that the mass concentration of the strong base and weak acid salt is 0.55%.
The neutral oils obtained in comparative examples 5 and 6 were examined and the results are shown in Table 3.
TABLE 3 detection and extraction of neutral oils of comparative examples 5 to 6
It can be seen from the above examples and comparative examples that the production process for extracting neutral oil from the pot bottom material provided by the invention can effectively improve the extraction rate of the neutral oil in the pot bottom material by controlling the concentration and the addition amount of the strong base and the weak acid salt, and the obtained neutral oil has good quality, meets the quality requirement of crude oil, and can be directly used as crude oil.
Although the present invention has been described in detail by referring to the preferred embodiments, the present invention is not limited thereto. Various equivalent modifications or substitutions can be made on the embodiments of the present invention by those skilled in the art without departing from the spirit and scope of the present invention, and these modifications or substitutions are within the scope of the present invention/any person skilled in the art can easily conceive of the changes or substitutions within the technical scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (8)
1. A production process for extracting neutral oil from tank bottoms is characterized by mainly comprising the following steps: preparing strong base weak acid salt solution with mass concentration of 0.25-0.5%; taking a pot bottom material, adding a strong base weak acid salt solution into the pot bottom material, wherein the volume-weight (ml/g) ratio of the strong base weak acid salt solution to the pot bottom material is 10-15:100, uniformly mixing to obtain a mixed solution, and centrifuging the mixed solution to obtain neutral oil; wherein, in the process of uniformly mixing, the temperature is controlled to be 25-35 ℃.
2. The process of claim 1, wherein said strong base weak acid salt solution is one of sodium bicarbonate, sodium acetate, sodium sulfite, potassium bicarbonate, potassium carbonate.
3. The process of claim 1, wherein the alkali weak acid salt solution has a mass concentration of 0.42% and the volume to weight (ml/g) ratio of the alkali weak acid salt solution to the tank bottom material is 12: 100.
4. A process for the production of neutral oil from can bottoms according to claim 1, wherein the blending temperature is 28 ℃.
5. A process for the production of neutral oil from a tank bottom according to any of claims 1 to 4, characterized in that the specific process is as follows:
(1) placing the tank bottom material in a stirring tank, then adding strong base weak acid salt solution according to the proportion, starting stirring at the stirring speed of 30-40r/min, and controlling the temperature in the stirring tank to obtain a mixed solution;
(2) centrifuging the mixed solution at 3500r/min 2000-3500r/min for 2-3min to obtain layered solution, and collecting the upper layer solution as neutral oil.
6. The process for producing neutral oil from a tank bottom according to claim 5, wherein in the step (1), the stirring process is divided into two stages, the first stage stirring speed is 30-33r/min, and the maintaining time is 25-35 min; the stirring speed of the second stage is 34-40r/min, and the maintaining time is 30-40 min.
7. The process for producing neutral oil from can bottoms according to claim 5, wherein in step (1), said strongly basic and weakly acidic salt solution is added in two portions, the first portion being 85-90% of the total amount of the strongly basic and weakly acidic salt solution, before the first stage of stirring; after the first stage of stirring is finished, the remaining strong base weak acid salt solution is added into the stirring tank.
8. The process for producing neutral oil from a tank bottom according to claim 5, wherein in the step (2), the centrifugal conditions of the mixed liquid are: centrifuging at 3000r/min for 2.5 min.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114657017A (en) * | 2022-02-28 | 2022-06-24 | 安徽省农业科学院农业工程研究所 | Processing technology of Chinese torreya fruits |
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| GB366969A (en) * | 1930-11-06 | 1932-02-08 | Alexander Ferguson Yuill | Improved method of extracting oil and other by-products from ground nut sludge |
| GB427680A (en) * | 1933-04-28 | 1935-04-29 | Metallgesellschaft Ag | Process for refining vegetable and animal oils and fats |
| US20020036171A1 (en) * | 2000-07-31 | 2002-03-28 | Komeisha Corporation | Treatment method of waste oil or waste edible oil |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB366969A (en) * | 1930-11-06 | 1932-02-08 | Alexander Ferguson Yuill | Improved method of extracting oil and other by-products from ground nut sludge |
| GB427680A (en) * | 1933-04-28 | 1935-04-29 | Metallgesellschaft Ag | Process for refining vegetable and animal oils and fats |
| US20020036171A1 (en) * | 2000-07-31 | 2002-03-28 | Komeisha Corporation | Treatment method of waste oil or waste edible oil |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114657017A (en) * | 2022-02-28 | 2022-06-24 | 安徽省农业科学院农业工程研究所 | Processing technology of Chinese torreya fruits |
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