CN215781653U - Incomplete extraction system of farming of food level rice protein - Google Patents
Incomplete extraction system of farming of food level rice protein Download PDFInfo
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- CN215781653U CN215781653U CN202121951102.3U CN202121951102U CN215781653U CN 215781653 U CN215781653 U CN 215781653U CN 202121951102 U CN202121951102 U CN 202121951102U CN 215781653 U CN215781653 U CN 215781653U
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Abstract
The utility model relates to a pesticide residue extraction system of food-grade rice protein, wherein a dry rice protein elephant trunk is connected with an inlet of a first extraction tank, an outlet of the first extraction tank is connected with an inlet of a first conveying pump, an outlet of the first conveying pump is connected with an inlet of a first horizontal screw centrifuge, a light phase outlet of the first horizontal screw centrifuge is connected with an evaporation unit, a heavy phase protein outlet of the first horizontal screw centrifuge is connected with a protein inlet of a second extraction tank, a solvent inlet of the second extraction tank is connected with an ethanol supply unit, an outlet of the second extraction tank is connected with an inlet of a second conveying pump, an outlet of the second conveying pump is connected with an inlet of the second horizontal screw centrifuge, a light phase outlet of the second horizontal screw centrifuge is connected with a solvent inlet of the first extraction tank, and a heavy phase protein outlet of the second horizontal screw centrifuge is connected with a protein inlet of a vacuum disc desolventizer. The rice protein prepared by the system can ensure biological activity, has high purity, and avoids pesticide residues such as organic chlorine, phenolic compounds and the like in the rice protein from exceeding the standard.
Description
Technical Field
The utility model relates to a rice protein preparation system, in particular to a pesticide residue extraction system for food-grade rice protein, and belongs to the technical field of rice protein manufacture.
Background
Pesticide residue is always a serious difficult point problem in rice and grain processing, a great part of pesticide used on rice crops is attached to the crops, and part of the pesticide in the environment can be absorbed by the crops, so that the residual pesticide can be directly transmitted to people and animals through the crop processing, and serious threat is generated to the health of the people.
The quality of rice protein is generally recognized as the highest among rice proteins, belongs to high-quality plant protein, has higher biological value than other proteins, has the nutritional value comparable to cow milk and eggs, has the characteristics of low sensitivity, reasonable amino acid composition and the like, and can be used as food for infants and special people. The rice protein also has a certain health care function, and researches show that the rice protein can reduce blood pressure, reduce cholesterol, resist cancers, prevent chronic diseases and the like.
In recent years, rice protein is used as a main flow product of rice deep processing, has a very wide application prospect, and is required to be used as an additive in the food industry, the health care product industry and even the medicine industry to produce nutrition supplement products for adults and infants. However, the rice protein as a rice deep-processing product also has the problem of pesticide residue, and the pesticide residue of the rice protein is more than that of rice, which is not beneficial to the preparation of food-grade rice protein. At present, a pesticide stripper is still adopted as a main method for solving the problem of pesticide residue, but the physical method cannot thoroughly remove the pesticide residue and cannot fundamentally solve the problem.
SUMMERY OF THE UTILITY MODEL
The utility model aims to overcome the problems in the prior art and provide a pesticide residue extraction system for food-grade rice protein, the prepared rice protein can ensure the biological activity, improve the protein purity and prevent pesticide residues such as organic chlorine, phenolic compounds and the like in the rice protein from exceeding the standard.
In order to solve the technical problems, the pesticide residue extraction system of the food-grade rice protein comprises a dry rice protein chute, the dry rice protein elephant trunk is connected with an inlet of the first extraction tank, an outlet of the first extraction tank is connected with an inlet of the first conveying pump, an outlet of the first conveying pump is connected with an inlet of the first horizontal screw centrifuge, a light phase outlet of the first horizontal screw centrifuge is connected with the evaporation unit, a heavy phase protein outlet of the first horizontal screw centrifuge is connected with a protein inlet of the second extraction tank, a solvent inlet of the second extraction tank is connected with the ethanol supply unit, an outlet of the second extraction tank is connected with an inlet of the second conveying pump, an outlet of the second conveying pump is connected with an inlet of the second horizontal screw centrifuge, a light phase outlet of the second horizontal screw centrifuge is connected with a solvent inlet of the first extraction tank, and a heavy phase protein outlet of the second horizontal screw centrifuge is connected with a protein inlet of the vacuum disc desolventizing machine.
As an improvement of the utility model, an outlet of the vacuum disc desolventizing machine is connected with an inlet of a first brake dragon, a discharge port of the first brake dragon is connected with an inlet of a first buffer bin through a permanent magnet cylinder, an exhaust port of the first brake dragon is connected with an inlet of a first pulse dust collector, an outlet of the first pulse dust collector and an outlet of the first buffer bin are connected with an inlet of a superfine pulverizer together, an outlet of the superfine pulverizer is connected with an inlet of a second brake dragon, a discharge port of the second brake dragon is connected with an inlet of a second buffer bin, an exhaust port of the second brake dragon is connected with an inlet of a second pulse dust collector, and an outlet of the second pulse dust collector and an outlet of the second buffer bin are connected with a packing system together.
As a further improvement of the utility model, an exhaust port of the vacuum disc desolventizer is connected with an inlet of a wet trap, an exhaust port of the wet trap is connected with a shell pass inlet of a pre-evaporator, and a shell pass outlet of the pre-evaporator is connected with an inlet of an evaporative condenser; the light phase outlet of the first horizontal decanter centrifuge is connected with the tube side inlet of the pre-evaporator, the tube side outlet of the pre-evaporator is connected with the inlet of the pre-evaporation flash tank, the top outlet of the pre-evaporation flash tank is connected with the inlet of the evaporative condenser, and the liquid phase outlet of the evaporative condenser is connected with the ethanol supply unit through an ethanol return pipe.
As a further improvement of the utility model, the liquid phase of the pre-evaporation flash tank is connected with the inlet of a third delivery pump, the outlet of the third delivery pump is connected with the inlet at the upper part of an evaporator, the lower part of the evaporator is communicated with a steam-water separator, and the outlet at the top part of the steam-water separator is connected with the inlet of the evaporation condenser; and an outlet at the bottom of the evaporator is connected with an inlet of a fourth delivery pump, and an outlet of the fourth delivery pump is connected with the ethanol return pipe.
As a further improvement of the utility model, the shell-side liquid phase outlet of the pre-evaporator is connected with the ethanol return pipe.
As a further improvement of the utility model, the heat medium inlets of the first extraction tank, the second extraction tank and the vacuum disk desolventizer are connected with a flash evaporation steam pipe of the liquefaction unit.
Compared with the prior art, the utility model has the following beneficial effects: the utility model adopts two-stage extraction, uses high-concentration ethanol solution as extraction liquid, heats up and soaks rice protein, fully extracts and peels pesticide residues in the protein, cleans organic pesticide, extracts the pesticide residues into the ethanol solution, thoroughly separates the pesticide residues and the rice protein by using a horizontal screw centrifuge, and then desolventizes and dries the rice protein. The whole system adopts a low-temperature and closed mode, so that the rice protein meets the food-grade requirement, the horizontal screw has high tightness, the ethanol solution is prevented from overflowing, the rice protein is prevented from being polluted by the environment, the environment is prevented from being polluted by the ethanol solution, the heating area of the vacuum disc desolventizing machine adopted for desolventizing the rice protein is large and uniform, the protein can be prevented from being bonded by stirring fins in equipment, the activity of the rice protein is prevented from being influenced at low temperature, the stability of the equipment is high, and the safety is good. If the extracted ethanol solution reaches a certain concentration, pollution discharge is carried out, if the concentration of pesticide residues is low, the ethanol solution is recycled, evaporated and concentrated, and then the mixture ratio is recycled, so that the full utilization of energy is ensured, the whole extraction process is reverse extraction, the consumption of fresh ethanol can be saved, the ethanol solution is fully utilized, and the energy waste is avoided. The whole pesticide residue extraction system can not damage the secondary structure of the rice protein, does not influence the activity of the protein, and meets the requirement of food grade.
Drawings
The utility model will be described in further detail with reference to the following drawings and detailed description, which are provided for reference and illustration purposes only and are not intended to limit the utility model.
FIG. 1 is a flow diagram of the pesticide residue extraction system for food grade rice protein of the present invention.
In the figure: 1. a first extraction tank; 2. a first delivery pump; 3. a first horizontal decanter centrifuge; 4. a second extraction tank; 5. a second delivery pump; 6. a second horizontal decanter centrifuge; 7. a vacuum disc desolventizing machine; 8. a first brake dragon; 9. a first pulse dust collector; 10. a permanent magnet drum; 11. a first surge bin; 12. an ultrafine pulverizer; 13. a second brake Kelong; 14. a second pulse dust collector; 15. a second surge bin; 16. a packaging system; 17. a wet trap; 18. a pre-evaporator; 19. pre-evaporating a flash tank; 20. a third delivery pump; 21. an evaporator; 22. a steam-water separator; 23. a fourth delivery pump; 24. an evaporative condenser; G1. a dried rice protein elephant trunk; G2. a steam pipe; G3. an ethanol reflux pipe.
Detailed Description
As shown in fig. 1, the system for extracting pesticide residues from food-grade rice protein comprises a dry rice protein elephant trunk G1, wherein the dry rice protein elephant trunk G1 is connected with an inlet of a first extraction tank 1, an outlet of the first extraction tank 1 is connected with an inlet of a first conveying pump 2, an outlet of the first conveying pump 2 is connected with an inlet of a first horizontal decanter centrifuge 3, a light phase outlet of the first horizontal decanter centrifuge 3 is connected with an evaporation unit, a heavy phase protein outlet of the first horizontal decanter centrifuge 3 is connected with a protein inlet of a second extraction tank 4, a solvent inlet of the second extraction tank 4 is connected with an ethanol supply unit, an outlet of the second extraction tank 4 is connected with an inlet of a second conveying pump 5, an outlet of the second conveying pump 5 is connected with an inlet of a second horizontal decanter centrifuge 6, a light phase outlet of the second horizontal decanter centrifuge 6 is connected with a solvent inlet of the first extraction tank 1, and a heavy phase protein outlet of the second horizontal decanter centrifuge 6 is connected with a protein inlet of a vacuum disk desolventizer 7.
The export of vacuum disc desolventizing machine 7 links to each other with the entry of first ke dragon 8 of stopping, the discharge opening of first ke dragon 8 of stopping links to each other through the entry of permanent magnetism section of thick bamboo 10 with first surge bin 11, the gas vent of first ke dragon 8 of stopping links to each other with the entry of first pulse dust collector 9, the export of first pulse dust collector 9 and the export of first surge bin 11 link to each other with the entry of super little rubbing crusher 12 jointly, the export of super little rubbing crusher 12 links to each other with the entry of second ke dragon 13, the discharge opening of second ke dragon 13 of stopping links to each other with the entry of second surge bin 15, the gas vent of second ke dragon 13 of stopping links to each other with the entry of second pulse dust collector 14, the export of second pulse dust collector 14 links to each other with the package system 16 jointly with the export of second surge bin 15.
An exhaust port of the vacuum disc desolventizer 7 is connected with an inlet of a wet trap 17, an exhaust port of the wet trap 17 is connected with a shell pass inlet of a pre-evaporator 18, and a shell pass outlet of the pre-evaporator 18 is connected with an inlet of an evaporative condenser 24; the light phase outlet of the first horizontal decanter centrifuge 3 is connected with the tube side inlet of the pre-evaporator 18, the tube side outlet of the pre-evaporator 18 is connected with the inlet of the pre-evaporation flash tank 19, the top outlet of the pre-evaporation flash tank 19 is connected with the inlet of the evaporative condenser 24, and the liquid phase outlet of the evaporative condenser 24 is connected with the ethanol supply unit through an ethanol return pipe G3.
The liquid phase of the pre-evaporation flash tank 19 is connected with the inlet of a third delivery pump 20, the outlet of the third delivery pump 20 is connected with the inlet of the upper part of an evaporator 21, the lower part of the evaporator 21 is communicated with a steam-water separator 22, and the outlet of the top part of the steam-water separator 22 is connected with the inlet of an evaporation condenser 24; the bottom outlet of the evaporator 21 is connected to the inlet of the fourth feed pump 23, and the outlet of the fourth feed pump 23 is connected to an ethanol return pipe G3.
The shell-side liquid phase outlet of the pre-evaporator 18 is connected to an ethanol return pipe G3. The steam pipe G2 provides a heat source for the first extraction tank 1 and the second extraction tank 4, and heat medium inlets of the first extraction tank 1, the second extraction tank 4 and the vacuum disc desolventizer 7 can also be connected with a flash evaporation steam pipe of the liquefaction unit, and the flash evaporation steam of the liquefaction unit is used as the heat source, so that the gradient recycling of heat energy is realized.
In the rice planting process, organic chlorine, phenolic compound pesticides and the like possibly exceed standards, so that the dried protein is extracted by two stages of countercurrent extraction. Dry rice protein from dry rice protein chute G1 was first introduced into first extraction tank 1, mixed with 95% ethanol solution at a solid to liquid ratio of 1: and 4, leaching for 60min at the temperature of 60 ℃, then conveying the leached protein into a first horizontal screw centrifuge 3 through a first conveying pump 2 for primary separation, feeding heavy-phase protein separated by the first horizontal screw centrifuge 3 into a second extraction tank 4 for secondary extraction, and feeding light-phase clarified liquid separated by the first horizontal screw centrifuge 3 into a subsequent evaporation unit for concentration and recycling.
And the second extraction tank 4 is filled with 95% ethanol solution again in a solid-to-liquid ratio of 1: and 4, leaching for 60min at the temperature of 60 ℃, then conveying the mixture into a second horizontal screw centrifuge 6 through a second conveying pump 5 for secondary separation, and carrying out nitrogen gas inflation explosion prevention on the first horizontal screw centrifuge 3 and the second horizontal screw centrifuge 6 so as to completely separate pesticide residues and rice protein. The heavy phase protein separated by the second horizontal decanter centrifuge 6 enters a vacuum disc desolventizing machine 7 for ethanol desolventizing at the temperature of about 80 ℃; the light phase clarified liquid separated by the second horizontal screw centrifuge 6 flows back to the first extraction tank 1 to realize counter-current washing.
And the first horizontal screw centrifuge 3 and the second horizontal screw centrifuge 6 are connected with a sewage discharge pipeline when the light phases are the same, if the content of pesticides such as organic chlorine and phenolic compounds exceeds the standard, the pesticides are soaked and eluted twice by ethanol, the pesticides are dissolved out of protein and carried into ethanol solution, when the concentration of the pesticides in the ethanol solution exceeds 0.1mg/kg, sewage discharge is carried out, and if the concentration of the pesticides in the ethanol solution is less than 0.1mg/kg, the pollutants are recycled.
Ethanol steam generated in the desolventizing process of the vacuum disc desolventizer 7 enters a wet trap 17 to be collected, enters a shell pass of a pre-evaporator 18, and enters an evaporation condenser 24 to be condensed into liquid ethanol after heat exchange and temperature reduction. The light phase clarified liquid separated by the first horizontal decanter centrifuge 3 enters the tube pass of the pre-evaporator 18, enters the pre-evaporation flash tank 19 for flash evaporation after heat exchange and temperature rise, the ethanol steam flashed out enters the evaporation condenser 24 and is condensed into liquid ethanol, the liquid ethanol discharged from the bottom of the pre-evaporation flash tank 19 is sent into the evaporator 21 and the steam-water separator 22 by the third delivery pump 20 for evaporation again, the ethanol steam discharged from the top of the steam-water separator 22 also enters the evaporation condenser 24 and is condensed into liquid ethanol, the liquid ethanol discharged from the evaporation condenser 24 returns to the ethanol supply unit through an ethanol return pipe G3, and the ethanol is supplied to the second extraction tank 4. The liquid ethanol discharged from the bottom of the shell pass of the pre-evaporator 18 is returned to the ethanol supply unit through an ethanol return pipe G3, the liquid ethanol discharged from the bottoms of the evaporator 21 and the steam-water separator 22 is also sent to an ethanol return pipe G3 by a fourth delivery pump 23 and returned to the ethanol supply unit, and the ethanol is supplied to the second extraction tank 4, so that the stepped utilization is realized.
The heavy-phase protein after the ethanol exsolution enters a first stopping Kelong 8 for separation, is discharged to a permanent magnetic drum 10 for magnetic separation, falls into a first buffer bin 11 for temporary storage, enters a superfine crusher 12 for crushing, is discharged to a second buffer bin 15 for temporary storage after being separated by a second stopping Kelong 13, and is prepared to enter a packing system 16. The first stopping dragon 8 is matched with a first pulse dust collector 9 to recover materials overflowing from the top of the first stopping dragon 8, and the second stopping dragon 13 is matched with a second pulse dust collector 14 to recover materials overflowing from the top of the second stopping dragon 13.
The above description is only a preferred embodiment of the present invention, and not intended to limit the scope of the present invention. In addition to the above embodiments, the present invention may have other embodiments. All technical solutions formed by adopting equivalent substitutions or equivalent transformations fall within the protection scope of the claims of the present invention. Technical features of the present invention which are not described may be implemented by or using the prior art, and will not be described herein.
Claims (6)
1. The utility model provides a incomplete extraction system of farming of food level rice protein, includes dry rice protein elephant trunk, its characterized in that: the dry rice protein elephant trunk is connected with an inlet of the first extraction tank, an outlet of the first extraction tank is connected with an inlet of the first conveying pump, an outlet of the first conveying pump is connected with an inlet of the first horizontal screw centrifuge, a light phase outlet of the first horizontal screw centrifuge is connected with the evaporation unit, a heavy phase protein outlet of the first horizontal screw centrifuge is connected with a protein inlet of the second extraction tank, a solvent inlet of the second extraction tank is connected with the ethanol supply unit, an outlet of the second extraction tank is connected with an inlet of the second conveying pump, an outlet of the second conveying pump is connected with an inlet of the second horizontal screw centrifuge, a light phase outlet of the second horizontal screw centrifuge is connected with a solvent inlet of the first extraction tank, and a heavy phase protein outlet of the second horizontal screw centrifuge is connected with a protein inlet of the vacuum disc desolventizing machine.
2. The system for pesticide residue extraction of food grade rice protein of claim 1, wherein: the export of vacuum disc desolventizing machine links to each other with the first entry of stopping the dragon, the first discharge opening of stopping the dragon links to each other through the entry of a permanent magnetism section of thick bamboo with first surge bin, the first gas vent of stopping the dragon links to each other with the entry of first pulse dust remover, the export of first pulse dust remover links to each other with the entry of superfine pulverizer jointly with the export of first surge bin, the export of superfine pulverizer links to each other with the second entry of stopping the dragon, the second is stopped the dragon discharge opening and is linked to each other with the entry of second surge bin, the second is stopped the dragon's gas vent and is linked to each other with the entry of second pulse dust remover, the export of second pulse dust remover links to each other with the package system jointly with the export of second surge bin.
3. The system for pesticide residue extraction of food grade rice protein of claim 2, wherein: an exhaust port of the vacuum disc desolventizing machine is connected with an inlet of a wet trap, an exhaust port of the wet trap is connected with a shell pass inlet of a pre-evaporator, and a shell pass outlet of the pre-evaporator is connected with an inlet of an evaporative condenser; the light phase outlet of the first horizontal decanter centrifuge is connected with the tube side inlet of the pre-evaporator, the tube side outlet of the pre-evaporator is connected with the inlet of the pre-evaporation flash tank, the top outlet of the pre-evaporation flash tank is connected with the inlet of the evaporative condenser, and the liquid phase outlet of the evaporative condenser is connected with the ethanol supply unit through an ethanol return pipe.
4. The system for pesticide residue extraction of food grade rice protein of claim 3, wherein: the liquid phase of the pre-evaporation flash tank is connected with an inlet of a third delivery pump, an outlet of the third delivery pump is connected with an inlet at the upper part of an evaporator, the lower part of the evaporator is communicated with a steam-water separator, and an outlet at the top part of the steam-water separator is connected with an inlet of the evaporation condenser; and an outlet at the bottom of the evaporator is connected with an inlet of a fourth delivery pump, and an outlet of the fourth delivery pump is connected with the ethanol return pipe.
5. The system for pesticide residue extraction of food grade rice protein of claim 4, wherein: and a shell-side liquid phase outlet of the pre-evaporator is connected with the ethanol return pipe.
6. The pesticide residue extraction system of food grade rice protein as claimed in any one of claims 1 to 5, wherein: and the heat medium inlets of the first extraction tank, the second extraction tank and the vacuum disc desolventizer are connected with a flash evaporation steam pipe of the liquefaction unit.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121951102.3U CN215781653U (en) | 2021-08-19 | 2021-08-19 | Incomplete extraction system of farming of food level rice protein |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202121951102.3U CN215781653U (en) | 2021-08-19 | 2021-08-19 | Incomplete extraction system of farming of food level rice protein |
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| CN215781653U true CN215781653U (en) | 2022-02-11 |
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| CN202121951102.3U Active CN215781653U (en) | 2021-08-19 | 2021-08-19 | Incomplete extraction system of farming of food level rice protein |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114849278A (en) * | 2022-04-20 | 2022-08-05 | 山东省产品质量检验研究院 | Multi-stage extractor for separating saturated hydrocarbon and unsaturated hydrocarbon in oil product |
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2021
- 2021-08-19 CN CN202121951102.3U patent/CN215781653U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114849278A (en) * | 2022-04-20 | 2022-08-05 | 山东省产品质量检验研究院 | Multi-stage extractor for separating saturated hydrocarbon and unsaturated hydrocarbon in oil product |
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