CN113563970A - Production process for reducing amount of oil smoke of refined edible vegetable oil - Google Patents
Production process for reducing amount of oil smoke of refined edible vegetable oil Download PDFInfo
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- CN113563970A CN113563970A CN202110936530.7A CN202110936530A CN113563970A CN 113563970 A CN113563970 A CN 113563970A CN 202110936530 A CN202110936530 A CN 202110936530A CN 113563970 A CN113563970 A CN 113563970A
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- 239000008157 edible vegetable oil Substances 0.000 title claims abstract description 27
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 18
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- 235000019482 Palm oil Nutrition 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
-
- 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
- C11B3/001—Refining fats or fatty oils by a combination of two or more of the means hereafter
-
- 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
- C11B3/06—Refining fats or fatty oils by chemical reaction with bases
-
- 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
- C11B3/10—Refining fats or fatty oils by adsorption
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Microbiology (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Wood Science & Technology (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Fats And Perfumes (AREA)
- Edible Oils And Fats (AREA)
Abstract
The invention provides a production process for reducing the amount of refined edible vegetable oil fume, which adopts novel cavitation and steam explosion mixing neutralization reaction equipment and a neutralization method, wherein a cavity is arranged in an equipment shell, one end of the cavity is connected with a liquid inlet, the other end of the cavity is provided with a movable push rod, the head part of the push rod is provided with an umbrella-shaped flow guide head, one end of the cavity of the shell, which is close to the liquid inlet, is provided with a transition block, the transition block comprises a hollow structure, the size of an opening at one side close to the liquid inlet is smaller than that of an opening at one side far away from the liquid inlet, the minimum sectional area formed between the outermost end of the flow guide head and the transition block is smaller than that of the liquid inlet, and the side wall of the shell at the rear end of the transition block is provided with a liquid outlet. The distance between the umbrella-shaped flow guide head and the transition block can be adjusted by rotating the first push rod and the second push rod, so that a low-pressure area is formed between the umbrella-shaped flow guide head and the transition block, and cavitation neutralization is carried out through high-pressure and low-pressure conversion, so that the chemical reaction is carried out more thoroughly.
Description
Technical Field
The invention relates to the technical field of oil processing, in particular to a production process for reducing the oil smoke amount of refined edible vegetable oil.
Background
The refined edible vegetable oil is a necessary seasoning in daily life, but the refined edible vegetable oil on the market generally has the phenomenon of large amount of oil smoke. The components of the refined edible plant oil smoke are very complex, and researches show that at least more than 300 components are detected in the edible plant oil smoke, mainly comprise aromatic compounds and heterocyclic compounds such as fatty acid, alkane, olefin, aldehyde, ketone, alcohol, ester and the like, and at least dozens of the aromatic compounds and the heterocyclic compounds are harmful to human health.
Pure triglyceride (i.e. neutral oil) is not easy to volatilize, but in the actual oil product, besides triglyceride, a small amount of non-triglyceride components are easy to generate oil smoke in the heating process, wherein the non-triglyceride components comprise components which are easy to volatilize when the oil and fat are heated, such as free fatty acid, low-carbon chain aldehyde, ketone and the like, components which are easy to generate thermal decomposition to generate volatile substances, such as phospholipid, saccharide, monoglyceride and the like, and components which can promote the oil and fat to generate thermal decomposition, such as trace metal oxidation promoting agents such as copper, iron and the like.
These components are volatilized into the air in the process of heating the oil, and the oil can cause great harm to the health after being inhaled by a human body, so that the development of the stable oil with low oil smoke content is urgently needed to meet the health requirements of consumers.
The traditional oil refining process is shown in figure 1 and mainly comprises four sections of neutralization, decoloration, winterization (dewaxing) and deodorization. The main purpose of the neutralization section is, among other things, to remove the non-glyceride components present in the crude oil, such as free fatty acids, metal ions, gums and some pigments. The currently common neutralization method mainly comprises the steps of adding acid and alkali, and referring to a process flow chart of a neutralization section shown in figure 2, after the acid and the alkali are added, the phosphorus content and the content of free fatty acid are reduced by stirring, mixing and filtering, but the method is difficult to reduce the phosphorus content of the neutralized oil to a very low level, and simultaneously, crude oil with low phosphorus content is difficult to remove, and the phospholipid content is an important factor influencing the smoke content of the refined edible vegetable oil. Therefore, there is a need to develop a process for producing refined edible vegetable oil with low oil smoke.
Disclosure of Invention
In order to solve the problems, the invention provides a production process for reducing the amount of the refined edible vegetable oil fume, namely, the fume is subjected to neutralization through cavitation and steam explosion, dewaxing is carried out through gradient cooling, decoloring is carried out through combination of novel adsorbent hydrated silicon dioxide and diatomite, and deodorization is carried out through a freezing vacuum system. The refined edible vegetable oil produced by the production process has the advantages of low phospholipid content, low oil smoke amount, economy, energy conservation and environmental protection.
The technical scheme of the invention is as follows:
in view of the fact that no relevant literature report on processing factors influencing the amount of oil smoke of edible oil is consulted at present. Therefore, the inventor is related to the processing process of edible oil, and considering that the amount of oil smoke (which is the concentration of thermal decomposition products generated by a unit mass sample at a certain temperature in a unit time when oil is heated) is one of the oil quality indexes, the processing links influencing the amount of oil smoke are determined as follows: degumming, dewaxing, decolorizing and deodorizing.
The traditional refining process is mainly suitable for treating certain oils with high FFA content (such as palm oil, coconut oil and the like), other oils and fats such as sunflower seed oil generally contain more impurities and have deep color due to oil varieties and pretreatment processes, particularly non-hydrated phospholipid (NHP) generally accounts for more than 50% of the phospholipid composition, phospholipid, pigment and trace metals must be removed from the oil in the first degumming section, and subsequent refining can be normally carried out only through complete degumming to obtain stable finished oil with low oil smoke content, so the degumming process is very critical.
The invention discloses a neutralization process for efficient dephosphorization, which utilizes a set of novel cavitation steam explosion mixing neutralization reaction equipment to improve the neutralization effect, and the basic principle of the equipment is that firstly degumming oil added with acid is led into the neutralization reaction equipment through a pump, and simultaneously alkali is added for neutralization reaction, the degumming oil is oil with water content of about 0.2 percent and comprises two liquid phases, wherein the water has low boiling point in a low-pressure area, the pressure of edible oil is reduced to the saturated vapor pressure of the water when the edible oil passes through a controllable steam explosion mixing reaction chamber of the equipment, the water in the oil is vaporized to form cavitation bubbles, when the sectional area of the oil passing through is increased, the pressure is increased (namely a high-pressure area), the cavitation bubbles can be collapsed, high-temperature, high-pressure and strong shock waves generated during collapse and high-speed micro jet flow enable a large amount of energy, shock waves and shearing forces to be released, the mixing strength and the contact area of alkali liquor and the degumming oil can be enhanced, the contact time of the alkali liquor and the neutral oil is shortened, weak bonds formed between non-hydrated phospholipid and calcium and magnesium ions in the oil can be broken instantly by strong shock waves, so that the non-hydrated phospholipid is converted into hydrated phospholipid, the arrangement of the phospholipid is changed by the strong shock waves, the separation is facilitated, the acid and alkali consumption is reduced, the phosphorus and soap content is reduced, the soapstock amount of a first centrifugal machine is greatly reduced, the loss caused by oil content of the soapstock is reduced, and the grease yield of a neutralization section is improved.
The utility model discloses a cavitation steam explosion mixes neutralization reaction equipment includes the shell, the inside cavity that is equipped with of shell, cavity one end is passed through the blanking cover and is connected the inlet, and the other end is equipped with the removal push rod, push rod head portion is equipped with umbrella-type water conservancy diversion head, the cavity of shell is close to inlet one end and is equipped with the transition piece, the transition piece includes hollow structure, is close to inlet one side opening size and is less than and keeps away from inlet one side opening size, the minimum sectional area that forms between water conservancy diversion head outermost end and the transition piece is less than the inlet sectional area, it has the liquid outlet to open on the shell lateral wall of transition piece rear end.
Further, the movable push rod comprises a first push rod and a second push rod, the first push rod is rotatably connected to the inner wall of the rear end of the shell, the second push rod is rotatably connected to the inside of the first push rod, the head portion of the second push rod extends out of the head portion of the first push rod, the head portions of the first push rod and the second push rod are respectively provided with an umbrella-shaped flow guide head, and the umbrella-shaped flow guide head of the head portion of the first push rod is larger than the umbrella-shaped flow guide head of the head portion of the second push rod.
Furthermore, the umbrella-shaped flow guide head comprises a conical structure, the inclination direction of the umbrella-shaped flow guide head faces the liquid flow direction, the maximum cross section size of the umbrella-shaped flow guide head at the head part of the first push rod is not smaller than the minimum opening size of the transition block, and the maximum cross section size of the umbrella-shaped flow guide head at the head part of the second push rod is not larger than the maximum opening size of the transition block. Preferably, the end with the smaller opening size of the transition block is aligned with the liquid inlet, and the end with the larger opening size is aligned with the inner edge of the liquid outlet.
The invention carries out grease neutralization operation through a novel cavitation and steam explosion mixing neutralization reaction device, can adjust the distance between the two umbrella-shaped flow guide heads and the front and back ends of the transition block by rotating the first push rod and the second push rod, and ensures that the sectional area formed between the two umbrella-shaped flow guide heads and the transition block is smaller than that of the liquid inlet, thereby forming a high-pressure area between the two umbrella-shaped flow guide heads and the transition block, forming a low-pressure area at the positions of the two umbrella-shaped flow guide heads, and carrying out cavitation neutralization through high-pressure and low-pressure conversion, so that the chemical reaction is carried out more thoroughly.
The device is developed aiming at the characteristics of phospholipid, and grease enters from a liquid inlet, passes through a low-pressure area between the flow guide head and the transition block, enters a high-pressure area between the two umbrella-shaped flow guide heads and the transition block, reacts and then flows out from the liquid outlet. The principle of the device is that pressure is adjusted through a push rod, so that water power generates cavitation, when cavitation occurs, cavitation bubbles are generated in a local low-pressure area of liquid, then flow along with the liquid, the cavitation bubbles in a later high-pressure area are rapidly collapsed, abnormal high temperature and high pressure are locally generated in a liquid environment with normal temperature and pressure, energy generated by instant adiabatic collapse of the cavitation bubbles can promote reaction, and chemical reaction achieves the effects of energy saving and efficiency improvement.
In particular, phospholipids are amphiphilic molecules that form micelles in the presence of water, hindering interactions with acids and bases; when hydrodynamic cavitation occurs, the low pressure zone causes water in the micelles to evaporate, so that the micelles break and the acid and base can easily contact the polar head of the phospholipid for reaction; when the material passes through the cavitation zone, the pressure is suddenly changed into normal pressure, and the phospholipid forms micelles again, but at the moment, because the energy is rapidly changed in laminar flow, the laminar flow changes the compactness of the heavy phase, so that the heavy phase can be better separated in a centrifugal machine.
Aiming at the cavitation and steam explosion mixing and neutralizing reaction equipment, the inventor designs a novel grease neutralizing method, the cavitation and steam explosion mixing and neutralizing reaction equipment is connected between an acid reaction tank and an alkali reaction tank, a push rod is pushed to a specified position, and a high-pressure small space is formed between an umbrella-shaped flow guide head at the head parts of the two push rods and a transition block. When the refined edible vegetable oil is cavitated and neutralized, the food-grade phosphoric acid with the concentration of 85 percent and the food-grade liquid caustic soda with the Baume degree of 16-22 are added into the oil, and the cavitation is generated by utilizing the high pressure and the low pressure in the cavitation steam explosion mixing and neutralizing reaction equipment, so that the chemical reaction is carried out more thoroughly. The traditional stirring device is omitted, the phosphorus content is reduced to a lower level by utilizing cavitation neutralization, and simultaneously, the energy consumption can be saved.
A process for reducing the smoke content of refined edible vegetable oil includes such steps as neutralizing oil, decoloring, dewaxing and deodorizing.
Further, the decoloring medium adopted in the decoloring procedure is the combination of hydrated silicon dioxide and diatomite, and the amount of the decoloring medium accounts for 0.2-0.3% of the mass of the crude oil.
Further, the ratio of the hydrated silicon dioxide to the diatomite is 1: 0.8-1.2. Hydrated silica is a solid, amorphous form of porous silica, SiO in dry matter2The purity of the product is more than 99 percent, the water content is 35 to 43 percent, and the product has strong adsorption capacity on impurities (such as phosphorus, soap, iron, copper, calcium, magnesium and the like) and risk substances (such as benzopyrene, aflatoxin and the like). The adsorption principle is as follows: surface pole of hydrated silicon dioxideThe oil has strong affinity to polar pollutants, when the oil is heated, the hydrated silicon dioxide adsorbs impurities in the oil, and after the oil is adsorbed for a period of time, the hydrated silicon dioxide is subjected to vacuum drying, at the moment, the water in the hydrated silicon dioxide is evaporated, and SiO2The particle size is reduced, polar contaminants are trapped in the voids, and the dried reduced particles are filtered off through a filter precoated with diatomaceous earth.
The hydrated silicon dioxide is combined with the diatomite for decolorization, so that impurities such as phosphorus, soap and the like can be better adsorbed, the step of water washing can be omitted, and the oil smoke amount caused by the impurities such as phosphorus and the like can be reduced again, so that the oil smoke amount can be better reduced.
In the dewaxing process, a plurality of crystallizing tanks are arranged, crude oil overflows from a first crystallizing tank to a last crystallizing tank one by one through the plurality of crystallizing tanks, the temperature of the sunflower seed oil is gradually reduced in a step-by-step overflow mode, and filtration is performed after crystallization and crystal growth to remove wax in the oil.
Meanwhile, a full-continuous automatic control dewaxing process is adopted to accurately and quantitatively add diatomite according to the wax content in the crude oil, monitor the wax content of the oil product in real time, improve the product quality, improve the production efficiency and reduce the emission. Specifically, a double-helix feeder is adopted to accurately and quantitatively add the crystallization aid (diatomite) into the crystallization tank, the speed of the feeder is linked with the oil inlet flow through a PLC, and the addition amount of the crystallization aid is controlled to be 0.5-1% of the oil weight. And the sampling is monitored in real time, oil products are sampled every 8 hours on line, the laboratory separates wax with different carbon numbers through a pretreatment silica gel column, a gas chromatography-flame ion detector is used for rapid quantitative detection, and process parameters can be adjusted in time according to the wax content of the oil products. For example, the frequency and amount of addition of the crystallization aid, the switching time and pressure of the horizontal filter, and the like.
In the production process for reducing the smoke amount of the refined edible vegetable oil, a freezing vacuum system is adopted for cooling in the deodorization procedure, and the temperature of the freezing water is between-20 ℃ and-35 ℃. The vacuum degree adjusting range is improved to be about 1.0-2.5 mbar, so that the optimum vacuum degree is more favorably found, the deodorization effect is improved, the quantity of the oil smoke can be further reduced, and meanwhile, compared with the traditional cooling water vacuum system, the steam consumption can be saved by 60-70%, and the electric energy can be saved by 10-20%.
Compared with the prior art, the invention has the advantages that:
1. the invention adopts novel cavitation steam explosion mixing neutralization reaction equipment to carry out neutralization operation, and utilizes high pressure and low pressure to generate cavitation, so that the chemical reaction is carried out more thoroughly, the phosphorus content in the grease is reduced to a lower level, and simultaneously, the energy consumption can be saved and the yield can be improved.
2. The production process for reducing the smoke volume of the refined edible vegetable oil comprises the steps of performing cavitation and steam explosion mixing neutralization, performing gradient cooling for dewaxing, combining novel adsorbent hydrated silicon dioxide and diatomite for decoloring, and performing deodorization by a freezing vacuum system, so that the smoke volume of the refined edible vegetable oil is reduced compared with that of the conventional production process, and the production process is economical, energy-saving and environment-friendly.
Drawings
The aspects and advantages of the present application will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the invention.
In the drawings:
FIG. 1 is a flow chart of a conventional oil refining process;
FIG. 2 is a process flow diagram of a conventional neutralization section;
FIG. 3 is a schematic structural diagram of a cavitation steam explosion mixing neutralization reaction device in the embodiment;
FIG. 4 is a graph showing the pressure change of a liquid passing through a cavitation and steam explosion mixing neutralization reaction apparatus;
FIG. 5 is a diagram showing the structure of phospholipid;
FIG. 6 is a diagram of the state of micelles formed by phospholipids before cavitation occurs in FIG. 1;
FIG. 7 is a diagram of the state of micelles formed by phospholipids before cavitation occurs in FIG. 2;
FIG. 8 is a graph showing changes in phospholipids in the low pressure region when air pressure occurs;
FIG. 9 is a graph of changes in phospholipid in the atmosphere after cavitation;
FIG. 10 shows the chemical reaction of a non-hydratable phospholipid NHP when converted to a HP hydratable phospholipid;
FIG. 11 is a schematic view showing the connection of a cavitation steam explosion mixing neutralization reaction apparatus in the grease neutralization process;
the components represented by the reference numerals in the figures are:
1. the device comprises a shell, 11, a blocking cover, 2, a first push rod, 21, a first flow guide head, 3, a second push rod, 31, a second flow guide head, 4, a flow inlet, 5, a flow outlet, 6, a transition block, 61 and a vortex reaction zone.
Detailed Description
Exemplary embodiments of the present disclosure will be described in more detail below with reference to the accompanying drawings. It should be noted that these embodiments are provided so that this disclosure can be more completely understood and fully conveyed to those skilled in the art, and the present disclosure may be implemented in various forms without being limited to the embodiments set forth herein.
Examples
In the production of refined edible vegetable oils, the neutralization method is usually mainly to add acid and alkali, then to mix and filter while stirring, to reduce the phosphorus content and the free fatty acid content, as shown in fig. 2. Acid degumming is to add phosphoric acid to convert non-hydrated phospholipid into hydrated phospholipid, chelate trace metals, reduce the content of trace metals in the grease and keep the stability of the grease. The phospholipids are removed by neutralization of the resulting soapstock, adsorption into agglomerates and centrifugation.
The principle of neutralization is to remove free fatty acid in grease by utilizing the neutralization reaction of free fatty acid and sodium hydroxide and acid-base to generate fatty acid salt and form soapstock.
However, conventional mixing by stirring is difficult to reduce the phosphorus content to a very low level, and is difficult to remove crude oil which is inherently low in phosphorus content.
Therefore, the inventor invents a novel cavitation and steam explosion mixing and neutralization reaction device, referring to fig. 3, which comprises a shell 1, wherein a cavity is arranged in the shell 1, one end of the cavity is connected with a liquid inlet 4, the other end of the cavity is provided with a combined type movable push rod, the movable push rod comprises a first push rod 2 and a second push rod 3, and the first push rod 2 is in threaded connection with the inner wall of the rear end of the shell 1.
Further, the inside of first push rod 2 is empty, and the back end is equipped with internal thread and external screw thread, second push rod 3 rotates to be connected inside first push rod 2, and the head stretches out from 2 heads of first push rod, first push rod 2 and 3 centers of second push rod align with 4 centers of inlet. The rear ends of the first push rod 2 and the second push rod 3 are provided with handles, and the rotating handles can respectively control the distance between the first push rod 2 and the second push rod 3 and the liquid inlet 4.
Furthermore, the first push rod 2 and the second push rod 3 are respectively connected with a first flow guide head 21 and a second flow guide head 31 through threads, the first flow guide head 21 and the second flow guide head 31 are both umbrella-shaped flow guide heads, the specific structure is a conical structure, the inclination direction faces to the liquid flow direction, and the maximum diameter is larger than the diameter of a connecting rod connected behind the conical structure.
Further, the cavity of shell 1 is close to 4 one ends of inlet and is equipped with transition piece 6, transition piece 6 is hollow structure, and central point puts and is equipped with the bell mouth, is close to 4 one sides opening size of inlet and is less than and keeps away from 4 one sides opening size of inlet, first water conservancy diversion head 21 with the minimum sectional area that forms between second water conservancy diversion head 31 outermost end and the transition piece 6 all is less than 4 sectional areas of inlet. Preferably, the maximum diameter of the second diversion head 31 is matched with the diameter of the liquid inlet 4, and the liquid flow at the position of the transition block 6 can be controlled to be changed from 0 to the maximum value.
Furthermore, a liquid outlet 5 is formed in the side wall of the shell 1 at the rear end of the transition block 6. The diameter of the liquid outlet 5 is the same as that of the liquid inlet 4, and the opening position of the liquid outlet is flush with the rear end of the transition block 6.
In the embodiment, the maximum diameter of the first flow guiding head 21 at the head part of the first push rod 2 is larger than that of the second flow guiding head 31 at the head part of the second push rod 3 so as to adapt to the change of the inclination of the transition block 6. The maximum cross-sectional dimension of the first flow guiding head 21 at the head of the first push rod 2 is smaller than the maximum opening dimension of the transition block 6.
Preferably, the smaller opening end of the transition block 6 is aligned with the liquid inlet 4, and the larger opening end is aligned with the inner edge of the liquid outlet 5. The liquid can flow smoothly from the liquid inlet 4 to the liquid outlet 5, and the resistance is reduced.
When the grease neutralizing operation is performed through the device, the first push rod 2 and the second push rod 3 are rotated firstly, and the distances between the first flow guide head 21, the second flow guide head 31 and the transition block 6 are adjusted, so that the cross-sectional areas between the first flow guide head 21 and the transition block 6 and between the second flow guide head 31 and the transition block 6 are smaller than the cross-sectional area of the liquid inlet 4, and the device is shown in fig. 4. The reduction of the cross section area increases the speed of the liquid flowing through the area, so that the pressure value at the area is lower than the pressure at the front side and the rear side, the pressure is reduced when the edible oil passes through the area to the saturated vapor pressure of water, the water in the oil is vaporized to form cavitation bubbles, the cavitation bubbles flow with the liquid, when the cross section area of the oil passing through the area is increased, the pressure is increased, namely the oil reaches a high-pressure area, the cavitation bubbles are collapsed, high-temperature, high-pressure and strong shock waves generated during collapse and high-speed micro jet flow release a large amount of energy, shock waves and shearing force, the mixing strength and the contact area of the alkali liquor and the degummed oil can be enhanced, the contact time of the alkali liquor and the neutral oil is shortened, the strong shock waves can instantaneously break weak bonds formed between the non-hydrated phospholipid and calcium and magnesium ions in the oil, so that the non-hydrated phospholipid is converted into hydrated phospholipid, the strong shock wave changes the arrangement of phospholipid, which is more beneficial to separation, thereby reducing the dosage of acid and alkali, reducing the content of phosphorus and soap, reducing the loss caused by the oil content of the soap and improving the yield.
Further, transition piece 6 intermediate position is equipped with a plurality of recesses, forms vortex reaction zone 61 in the recess position, first water conservancy diversion head 21 and second water conservancy diversion head 31 are located transition piece 6 a plurality of recesses's front and back both sides respectively, follow the liquid of low-pressure region entering high nip, can not flow out from first water conservancy diversion head 21 at once, and when the vortex reaction zone 61 was flowed through to liquid stream, the cavitation bubble met with the delay, had both guaranteed that the cavitation bubble is all broken at the high-pressure region, can not flow out from the low-pressure region, had still prolonged reaction time, promoted the emergence of reaction.
The principle of cavitation neutralization in the present apparatus will be described in detail with reference to FIGS. 5-9, in which the phospholipid is an amphiphilic molecule comprising a polar head and a hydrophobic tail, and forms micelles in the presence of water, which prevents interaction with acids and bases, and the liquid at the position of loading port 4 is shown in this state, see FIGS. 6 and 7.
When hydrodynamic cavitation occurs, i.e., the liquid flows through the low pressure zone, the low pressure zone causes the water in the micelles to evaporate under the action of the pressure differential, and thus the micelles break, and the acid and base can easily contact the polar head of the phospholipid for reaction. Referring to fig. 8, the liquid at the rear position of the second flow guiding head 31 assumes this state.
When the material passes through the cavitation zone, the pressure is suddenly changed into normal pressure, and the phospholipid forms micelles again, but at the moment, because the energy is rapidly changed in laminar flow, the laminar flow changes the compactness of the heavy phase, so that the heavy phase can be better separated in a centrifugal machine. Referring to fig. 9, the liquid in the front position of the first flow guiding head 21 is in this state.
During the hydration degumming process, water must be dispersed in the oil because of the excess water added, but the degree of dispersion is not critical. A reasonable dispersion has provided such an oil/water interface that the hydrated phospholipid hydrates and enters the aqueous phase. To react the acid with the non-hydratable phospholipid and break down the NHP, a finer dispersion is required because both reagents are diluted. Very fine dispersions are particularly required when the reaction has to be completed instantaneously and very low residual phospholipid contents have to be achieved. Moreover, if the oil-water dispersion is unstable, the reaction difficulty is increased, acid droplets will coalesce, the interface will decrease, and the diffusion distance will increase, all of which will slow down the reaction. Therefore, the dispersion must be fine in order for the reaction between the acid and the NHP to be almost instantaneous or at least almost complete within one minute.
Thus, the acid or base degumming effect is highly dependent on kinetic theory and on the instantaneous reaction efficiency. The cavitation system of this embodiment maximizes the interfacial area of water and oil and minimizes the diffusion distance to the interface for a given duration. Furthermore, the phospholipids reaching the interface may encounter only water, and only a few will find acid molecules dissolved in the water, so the cavitation neutralization system helps to provide a uniform chemical solution, maximizing the chances of hydration.
When the non-hydrated phospholipid NHP is converted into HP hydrated phospholipid, the cavitation reaction causes the anions to be carried away by the sodium of the anode, see figure 10, thereby reducing the total acid dosage, subsequently reducing the dosage of alkali liquor for neutralizing residual acid and further improving the grease yield.
Aiming at the cavitation and steam explosion mixing and neutralizing reaction equipment, the inventor designs a novel grease neutralizing method, and the cavitation and steam explosion mixing and neutralizing reaction equipment is connected between an acid reaction tank and an alkali reaction tank, and is shown in figure 11. When the device is used, the distance between the umbrella-shaped flow guide head and the transition block 6 can be adjusted by rotating the first push rod 2 and the second push rod 3, so that a low-pressure area is formed between the first flow guide head 21 and the transition block 6 and between the second flow guide head 31 and the transition block 6, the pressure is lower than the front side and the rear side, and the physical cavitation neutralization is carried out through high-pressure and low-pressure conversion, so that the chemical reaction is more thorough. The traditional stirring device is omitted, the phosphorus content is reduced to a lower level by utilizing cavitation neutralization, and simultaneously, the energy consumption can be saved.
Under the same working condition, the cavitation neutralization method is compared with the traditional mode of adding acid and alkali, and then stirring, mixing, filtering and neutralizing:
the phosphorus content in the neutralization section is reduced by 15ppm (about 50ppm in the traditional process);
the soap content after the first centrifugal machine in the neutralization section is reduced to 500ppm (about 650ppm in the traditional process);
the yield of the neutralization section is increased approximately: 0.3 percent;
the acid dosage is reduced: 50 percent;
the alkali dosage is reduced: 40 percent;
and the cavitation equipment in the neutralization section does not need to be provided with a CIP (cleaning in place) process, has no blocking risk, is easy to operate, and is safe and reliable.
The invention also provides a production process for reducing the smoke amount of the refined edible vegetable oil, which comprises the oil neutralization method and the working procedures of decolorization, dewaxing and deodorization.
Furthermore, a novel adsorbent is adopted in the decoloring procedure for decoloring.
At present, the decolorization is mainly carried out by adsorbing impurities such as pigments, phosphorus, soaps and the like and risk substances by using activated clay, but the higher the activity degree of the activated clay is, the higher the addition amount is, the larger the oil smoke amount is, so that a novel adsorbent needs to be developed to replace or be combined with diatomite for use.
Hydrated silica is a solid, amorphous, porous hydrated silica form, SiO in dry matter2The purity of the product is more than 99%, and the product has strong adsorption capacity on impurities (such as phosphorus, soap, iron, copper, calcium, magnesium and the like) and risk substances (such as benzopyrene, aflatoxin and the like). The adsorption principle is as follows: the surface polarity of the hydrated silicon dioxide has strong affinity to polar pollutants, when the oil is heated, the hydrated silicon dioxide adsorbs impurities in the oil, after the oil is adsorbed for a period of time, the hydrated silicon dioxide is subjected to vacuum drying, the water in the hydrated silicon dioxide is evaporated, and SiO2The particle size is reduced, polar contaminants are trapped in the voids, and the dried reduced particles are filtered off through a filter precoated with diatomaceous earth.
In this embodiment, 0.08% hydrated silica is used in combination with 0.05% diatomite for decolorization, so that impurities such as phosphorus and soap can be better adsorbed, the step of washing with water can be omitted, and the amount of oil smoke caused by impurities such as phosphorus can be reduced, so that the amount of oil smoke can be better reduced, as shown in the experimental data in table 1 below.
TABLE 1
Furthermore, in the dewaxing procedure, a full-continuous automatic control accurate quantitative addition dewaxing mode is adopted.
Waxes are high carbon chain fatty acid esters of higher monocarboxylic acids and higher monohydric alcohols, and these fatty acid esters are prone to soot formation. In general, the traditional domestic manual continuous dewaxing process is to cool an oil product to about 5 ℃ in a single crystallization tank, maintain the temperature for 24 hours and then filter the oil product to finish dewaxing. The defects are insufficient crystallization and poor dewaxing effect, and the quality of the dewaxed oil is influenced.
Meanwhile, a full-continuous automatic control dewaxing process is adopted to accurately and quantitatively add diatomite according to the wax content in the crude oil, monitor the wax content of the oil product in real time, improve the product quality, improve the production efficiency and reduce the emission. Specifically, a double-helix feeder is adopted to accurately and quantitatively add the crystallization aid (diatomite) into the crystallization tank, the speed of the feeder is linked with the oil inlet flow through a PLC, and the addition amount of the crystallization aid is controlled to be 0.7% of the oil weight. And the sampling is monitored in real time, oil products are sampled every 8 hours on line, the laboratory separates wax with different carbon numbers through a pretreatment silica gel column, a gas chromatography-flame ion detector is used for rapid quantitative detection, and process parameters can be adjusted in time according to the wax content of the oil products. For example, the frequency and amount of addition of the crystallization aid, the switching time and pressure of the horizontal filter, and the like.
Furthermore, a plurality of crystallizing tanks are arranged in the dewaxing procedure, for example, crude sunflower seed oil is taken as an example, the crude oil overflows one by one from a first crystallizing tank to a last crystallizing tank through the plurality of crystallizing tanks, the temperature of the crude oil is gradually reduced in the overflow process, and the crude oil is filtered after crystallization and crystal growth to remove wax in the oil.
Test example: by accurately and quantitatively adding 0.7% of diatomite crystallization promoter, 100 tons of sunflower seed crude oil is processed, 80kg of diatomite can be saved by low-content wax (220mg/kg) and high-content wax (360mg/kg), the cost (the dosage of the diatomite and the treatment cost of the waste diatomite) is saved by 15.29%, and the refining yield is increased by 0.2-0.5%.
Comparative example: referring to the comparative experimental data of the present example and the conventional dewaxing process in the following table 2, it can be seen that the dewaxing effect can be improved by 1 time by fully-continuous self-control precise quantitative addition and real-time monitoring of the wax content in the production process. Therefore, the full-continuous automatic control accurate quantitative dewaxing process can reduce the oil smoke amount of the refined edible vegetable oil.
TABLE 2
In the production process for reducing the amount of the refined edible vegetable oil fume, a freezing vacuum system is adopted for deodorization in the deodorization procedure.
The deodorization is a process of removing odor substances by steam distillation under the conditions of high temperature and high vacuum degree by utilizing the difference of the volatility of the odor substances and the fatty acid triglyceride in the grease. The quality of the deodorization effect directly influences the oil smoke amount of the product, and the quality and the stability of the vacuum degree directly influence the deodorization effect. At present, the vacuum system commonly used is cooling water vacuum system, but this vacuum system vacuum degree regulation interval is less (1.0 ~ 1.5mbar), and the vacuum degree is unstable, can influence the deodorization effect, and then influences the oil smoke volume.
The freezing vacuum system is cooled by using freezing water (20 ℃ below zero to 35 ℃ below zero), the adjustment range of the vacuum degree is large (1.0-2.5 mbar), the optimal vacuum degree is more favorably found, the deodorization effect is improved, the quantity of the oil smoke can be further reduced, and meanwhile, compared with the steam consumption of the cooling water vacuum system, the steam consumption can be saved by 60-70%, and the electric energy can be saved by 10-20%.
In addition, the main steam source and the vacuum degree of the deodorization tower are automatically controlled by a PLC (programmable logic controller), the vacuum degree of the deodorization tower can be monitored in real time, and the steam consumption can be adjusted at any time according to the vacuum degree of the deodorization tower, so that the stability of the vacuum degree of the deodorization tower is maintained, the deodorization effect is improved, and the oil smoke quantity is reduced.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any changes or additions or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are also included in the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the appended claims.
Claims (10)
1. The utility model provides a cavitation steam explosion mixes neutralization reaction equipment, a serial communication port, including shell (1), shell (1) inside is equipped with the cavity, inlet (4) are connected to cavity one end, and the other end is equipped with the removal push rod, push rod head is equipped with umbrella-type water conservancy diversion head, the cavity of shell (1) is close to inlet (4) one end and is equipped with transition piece (6), transition piece (6) are less than and keep away from inlet (4) one side opening size including hollow structure, are close to inlet (4) one side opening size, the minimum sectional area that forms between water conservancy diversion head outermost end and transition piece (6) is less than inlet (4) sectional area, it has liquid outlet (5) to open on the shell lateral wall of transition piece (6) rear end.
2. The cavitation and steam explosion mixing neutralization reaction equipment is characterized in that the movable push rod comprises a first push rod (2) and a second push rod (3), the first push rod (2) is rotatably connected to the inner wall of the rear end of the shell (1), the second push rod (3) is rotatably connected to the inside of the first push rod (2), the head of the second push rod extends out of the head of the first push rod (2), umbrella-shaped flow guide heads are arranged at the heads of the first push rod (2) and the second push rod (3), and the umbrella-shaped flow guide head at the head of the first push rod (2) is larger than the umbrella-shaped flow guide head at the head of the second push rod (3).
3. The cavitation steam explosion mixing and neutralization reaction device as recited in claim 2, characterized in that the umbrella-shaped flow guiding head comprises a conical structure, the inclination direction is towards the liquid flowing direction, the maximum cross-sectional dimension of the umbrella-shaped flow guiding head at the head part of the first push rod (2) is not smaller than the minimum opening dimension of the transition block (6), and the maximum cross-sectional dimension of the umbrella-shaped flow guiding head at the head part of the second push rod (3) is not larger than the maximum opening dimension of the transition block (6).
4. The cavitation steam explosion mixing and neutralizing reaction device as recited in claim 3, characterized in that the smaller opening end of the transition block (6) is aligned with the liquid inlet (4) and the larger opening end is aligned with the inner edge of the liquid outlet (5).
5. A grease neutralization method using the cavitation and steam explosion mixing and neutralization reaction device as defined in any one of claims 1 to 4, characterized in that the cavitation and steam explosion mixing and neutralization reaction device is connected between an acid reaction tank and an alkali reaction tank.
6. A process for reducing the smoke content of refined edible vegetable oil, which comprises an oil neutralization step, wherein the oil neutralization step adopts the oil neutralization method of claim 5, and further comprises the steps of decoloring, dewaxing and deodorizing.
7. The production process of reducing the amount of the fume of the refined edible vegetable oil as claimed in claim 6, wherein the decolorizing medium adopted in the decolorizing process is a combination of hydrated silica and diatomite, and the amount of the decolorizing medium accounts for 0.2-0.3% of the mass of the crude oil.
8. The production process for reducing the amount of the refined edible vegetable oil fume as claimed in claim 7, wherein the ratio of the hydrated silicon dioxide to the diatomite is 1: 0.6-1.0.
9. The process according to claim 6, wherein the dewaxing step comprises a plurality of crystallizers, the crude oil overflows from the first crystallizer to the last crystallizer one by one, the temperature of the sunflower seed oil is gradually reduced by means of gradual overflow, and the oil is crystallized, crystallized and filtered to remove the wax.
10. The process according to claim 6, wherein the deodorizing step is carried out by cooling with a freezing vacuum system at a temperature of-20 to-35 ℃.
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| CN104403792B (en) * | 2014-10-31 | 2016-07-27 | 南海油脂工业(赤湾)有限公司 | A kind of oils and fats continuous way Multi-stage cooling process for dewaxing and system |
| CA3011246C (en) * | 2016-01-19 | 2024-02-13 | Arisdyne Systems, Inc. | Method for degumming vegetable oil |
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2021
- 2021-08-16 CN CN202211124686.6A patent/CN115449427B/en active Active
- 2021-08-16 CN CN202110936530.7A patent/CN113563970A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114574287A (en) * | 2022-03-01 | 2022-06-03 | 北京华石联合能源科技发展有限公司 | Waste grease purification system and purification method |
| CN116240070A (en) * | 2022-05-04 | 2023-06-09 | 新纪元食品科技(佛山)有限公司 | Process for leaching grease |
Also Published As
| Publication number | Publication date |
|---|---|
| CN115449427A (en) | 2022-12-09 |
| CN115449427B (en) | 2024-02-09 |
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