Food-grade rice protein washing, refining and sterilizing device

Abstract

The utility model discloses a food-grade rice protein washing, refining and sterilizing device which comprises a first horizontal screw centrifuge connected with a protein pulp outlet, a protein outlet of the first horizontal screw centrifuge is connected with a first protein buffer tank, and a bottom outlet of the first protein buffer tank is connected with a cold side inlet of a heating heat exchanger through a pre-chelation protein delivery pump. An inlet of the pre-chelating protein delivery pump is further connected with an outlet of a citric acid discharge metering pump, a cold side outlet of the heating heat exchanger is connected with an inlet of a chelating tank, an outlet of the chelating tank is connected with an inlet of a second horizontal screw centrifuge through a post-chelating protein delivery pump, and a protein outlet of the second horizontal screw centrifuge is connected with a second protein buffer tank; a bottom outlet of the second protein buffer tank is connected with the protein sterilization unit through a refined protein slurry conveying pump; and an inlet of the refined protein slurry conveying pump is also connected with an outlet of a sodium carbonate discharge metering pump. The device can control harmful substances such as heavy metals in a food-grade standard range, and is low in energy consumption and safe and stable in production.

Description

Technical Field

[0001] The utility model relates to a broken rice processing system, in particular to a food-grade rice protein washing, refining and sterilizing device, belonging to the technical field of broken rice processing equipment. Background Art

[0002] In the process of rice processing, about 20% rice husks, 15% broken rice and 10% rice bran are produced as by-products. These by-products are rich in protein, fat, starch, etc. Normally, we use broken rice and rice bran as feed and rice husk as fuel, which not only wastes resources but also has a certain impact on the environment.

[0003] Rice protein is recognized as the best cereal protein. It is rich in essential amino acids, easily digested and absorbed by the human body, and has low allergenicity, making it very suitable for the development of infant products. Broken rice is of poorer quality than rice, with more impurities, high ash content, and relatively cheap price. However, broken rice also has its advantages, with a higher protein content relative to rice. The protein content of broken rice can reach about 10.5%, while the protein content of rice is about 8.8%, which is about 2 percentage points higher than that of normal rice.

[0004] In the traditional process, broken rice is used as raw material, and glucose and protein are obtained through cleaning, milling, liquefaction, saccharification, and filtration. At this time, the heavy metal content of the protein exceeds the standard and the content is low. Only a part of the syrup can be recovered by washing and then dried in a tube bundle to make feed-grade protein. The added value of the product is low, which affects the overall benefits of the enterprise.

[0005] In addition, protein high-temperature sterilization heat exchangers are prone to scaling and need to be frequently disassembled and cleaned, affecting continuous production. However, the direct heating and flash cooling method is prone to produce protein foam, causing the protein content in the flash steam to exceed the standard, affecting the quality of the condensed water, and the COD content in the condensed water is relatively high.

[0006] The Chinese invention patent application with publication number CN109303163 A discloses a method for extracting protein powder from broken rice, which takes the following steps: material preparation → grinding → slurry adjustment → liquefaction injection → deproteinization → protein washing → filtration → drying, etc. to produce protein powder. In this technical solution, protein purification only uses three times the volume of water for soaking, filtration and dehydration purification, because most of the heavy metals in rice will be transferred to the protein after liquid saccharification and separation, resulting in excessive heavy metal content in the protein; at the same time, in the subsequent protein filtration and purification process, a plate frame is used for dehydration, and the plate frame has many sanitary dead corners and cannot meet the requirements of food grade. Utility Model Content

[0007] The purpose of this section is to summarize some aspects of the embodiments of the utility model and briefly introduce some preferred embodiments. Some simplifications or omissions may be made in this section and the specification abstract and utility model name of this application to avoid blurring the purpose of this section, specification abstract and utility model name, and such simplifications or omissions cannot be used to limit the scope of the utility model.

[0008] In view of the above problems and / or the problems existing in the prior art, the present utility model is proposed.

[0009] The purpose of the utility model is to overcome the problems existing in the prior art and provide a food-grade rice protein washing, refining and sterilizing device, which can control harmful substances such as heavy metals within the food-grade standard range, has low energy consumption, and is safe and stable in production.

[0010] In order to solve the above technical problems, the utility model provides a food-grade rice protein washing, refining and sterilizing device, comprising a first decanter centrifuge connected to the protein slurry outlet of the liquefaction stage, the protein outlet of the first decanter centrifuge is connected to the first protein buffer tank, the bottom outlet of the first protein buffer tank is connected to the cold side inlet of the heating heat exchanger through a pre-chelating protein delivery pump, the inlet of the pre-chelating protein delivery pump is also connected to the outlet of the citric acid discharge metering pump, the cold side outlet of the heating heat exchanger is connected to the inlet of the chelating tank, the outlet of the chelating tank is connected to the inlet of the second decanter centrifuge through the post-chelating protein delivery pump, the protein outlet of the second decanter centrifuge is connected to the second protein buffer tank, the bottom outlet of the second protein buffer tank is connected to the protein sterilization unit through the refined protein slurry delivery pump, and the inlet of the refined protein slurry delivery pump is also connected to the outlet of the sodium carbonate discharge metering pump.

[0011] Furthermore, the tops of the first protein buffer tank and the second protein buffer tank are connected to RO water pipes via RO water regulating valves, respectively.

[0012] Furthermore, the clear liquid outlet of the first horizontal screw centrifuge is connected to a sugar water tank, and the bottom outlet of the sugar water tank is connected to a slurry water inlet of a grinding machine through a sugar water delivery pump.

[0013] Furthermore, the chelating tank is provided with two connected in series, each chelating tank is provided with at least two transverse partitions, and each transverse partition is evenly distributed with through holes.

[0014] Furthermore, the clear liquid outlet of the second horizontal screw centrifuge is connected to a sewage pipe.

[0015] Furthermore, the hot side inlet of the heating heat exchanger is connected to the steam pipeline through a steam regulating valve, and the opening of the steam regulating valve is controlled by the cold side outlet temperature of the heating heat exchanger.

[0016] Furthermore, the speed of the citric acid discharge metering pump is controlled by the pH value of the outlet of the pre-chelating protein delivery pump, and the speed of the sodium carbonate discharge metering pump is controlled by the pH value of the outlet of the refined protein slurry delivery pump.

[0017] Furthermore, the inlet pipes of the first decanter centrifuge and the second decanter centrifuge are respectively installed with regulating valves interlocked with the inlet flow rates.

[0018] Furthermore, the protein sterilization unit includes an ejector, a main inlet of the ejector is connected to the outlet of the refined protein slurry delivery pump, a steam inlet of the ejector is connected to a steam pipeline via an ejection steam regulating valve and a steam filter, an outlet of the ejector is connected to an inlet of a maintaining pipe, an outlet of the maintaining pipe is connected to an inlet of a side wall of a flash tank, a bottom outlet of the flash tank is connected to an inlet of a dehydration horizontal screw centrifuge via a post-flash delivery pump, and a protein outlet of the dehydration horizontal screw centrifuge is connected to a protein drying unit via a wet protein conveyor.

[0019] Furthermore, a defoaming device is provided on the top of the flash tank, and the flash steam outlet on the top is connected to the middle inlet of the gas-liquid separator, the bottom outlet of the gas-liquid separator is connected to the bottom pipeline of the flash tank, and the secondary steam outlet of the gas-liquid separator is connected to the heat source inlet of the triple-effect evaporator of the syrup evaporation and concentration unit.

[0020] Compared with the prior art, the utility model has achieved the following beneficial effects: 1. The protein filtered out during the processing of broken rice is further washed, chelated, and refined to remove impurities and excessive substances such as heavy metals so that the protein reaches food grade standards, thereby improving the yield of protein, turning waste into treasure, increasing the added value of products, and increasing factory profits.

[0021] 2. In view of the high impurities and ash content in broken rice, each production link is optimized during the processing to obtain high-quality rice protein, while increasing product added value by saving energy and reducing consumption.

[0022] 3. Use high-temperature direct jet heating for sterilization. The protein slurry is directly mixed with clean steam and heated to the required temperature. Maintain high-temperature sterilization for a certain period of time to avoid tube blockage and eliminate the need for frequent disassembly and cleaning.

[0023] 4. The sterilized protein enters the flash tank for flash cooling, and the cooled protein is removed from the horizontal screw for dehydration. In order to address the problem of foaming easily generated by flash evaporation of protein slurry, a defoaming device is added to the top of the flash tank. At the same time, the tail gas from the top of the flash tank is separated into gas and liquid again through a cyclone separator. The liquid brought out from the top is separated from the secondary steam by a cyclone separator. The secondary steam separated by two defoaming separations enters the evaporation system, reducing the consumption of steam generated by the evaporation system. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] In order to more clearly illustrate the technical solutions of the embodiments of the present utility model, the following will briefly introduce the drawings required for the description of the embodiments. Obviously, the drawings described below are only some embodiments of the present utility model. For ordinary technicians in this field, other drawings can be obtained based on these drawings without creative labor. The drawings are only provided for reference and explanation, not for limiting the present utility model. Among them:

[0025] Figure 1 This is a flow chart of the protein washing and refining unit in the utility model;

[0026] Figure 2 This is a flow chart of the protein sterilization unit in the utility model;

[0027] In the figure: protein washing and refining unit: steam pipeline 700; first horizontal screw centrifuge 801; feed regulating valve FC801; first protein buffer tank 802; RO water regulating valve FC802; pre-chelating protein delivery pump 803; heating heat exchanger 804; steam regulating valve TC804; chelating tank 805; post-chelating protein delivery pump 806; second horizontal screw centrifuge 807; post-chelating regulating valve FC807; second protein buffer tank 808; RO water regulating valve FC808; post-refining protein slurry delivery pump 809; citric acid tank 810; citric acid discharge metering pump 811; sodium carbonate tank 812; sodium carbonate discharge metering pump 813; sugar water tank 814; sugar water delivery pump 815;

[0028] Protein sterilization unit: ejector 901; jet steam regulating valve PC901; jet temperature sensor TT901; jet steam pressure sensor PA901; maintaining tube 902; steam filter 903; flash tank 904; gas-liquid separator 905; post-flash delivery pump 906; dehydration horizontal screw centrifuge 907; dehydration feed amount regulating valve FC907; wet protein conveyor 908. DETAILED DESCRIPTION

[0029] In the following description of the utility model, the terms "upper", "lower", "front", "back", "left", "right", "inside", "outside", etc. indicate directions or positional relationships based on the directions or positional relationships shown in the accompanying drawings. They are only for the convenience of describing the utility model and simplifying the description, and do not mean that the device must have a specific direction.

[0030] In order to make the technical means, creative features, objectives and effects of the present invention easier to understand, the present invention is further described below with reference to specific figures. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of them.

[0031] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as those commonly understood by those skilled in the art of the present invention. The terms used in the specification of the present invention are only for the purpose of describing specific embodiments and are not intended to limit the present invention.

[0032] The utility model discloses a food-grade rice protein washing, refining and sterilizing device, which comprises a protein washing and refining unit and a protein sterilizing unit.

[0033] like Figure 1 As shown, the protein washing and refining unit includes a first horizontal screw centrifuge 801, a first protein buffer tank 802, a heating heat exchanger 804, a chelating tank 805, a second horizontal screw centrifuge 807, a second protein buffer tank 808, a citric acid discharge metering pump 811, a sodium carbonate discharge metering pump 813 and a sugar water tank 814.

[0034] The protein slurry outlet of the liquefaction section is connected to the inlet of the first horizontal screw centrifuge 801, and the inlet pipeline of the first horizontal screw centrifuge 801 is installed with a feed regulating valve FC801 interlocked with the inlet flow.

[0035] The clear liquid outlet of the first horizontal screw centrifuge 801 is connected to the sugar water tank 814, and the bottom outlet of the sugar water tank 814 is connected to the slurry water inlet of the mill through the sugar water delivery pump 815.

[0036] The protein outlet of the first horizontal screw centrifuge 801 is connected to the first protein buffer tank 802 , the top of the first protein buffer tank 802 is connected to the RO water pipe through the RO water regulating valve FC802 , and the bottom outlet of the first protein buffer tank 802 is connected to the inlet of the pre-chelating protein delivery pump 803 .

[0037] The inlet pipe of the citric acid discharge metering pump 811 is inserted into the citric acid tank 810, and the outlet of the citric acid discharge metering pump 811 is also connected to the inlet of the pre-chelated protein delivery pump 803, and the rotation speed of the citric acid discharge metering pump 811 is controlled by the pH value of the outlet of the pre-chelated protein delivery pump 803.

[0038] The outlet of the pre-chelation protein delivery pump 803 is connected to the cold side inlet of the heating heat exchanger 804, and the hot side inlet of the heating heat exchanger 804 is connected to the steam pipeline 700 through the steam regulating valve TC804, and the opening of the steam regulating valve TC804 is controlled by the cold side outlet temperature of the heating heat exchanger 804. The cold side outlet of the heating heat exchanger 804 is connected to the inlet of the chelating tank 805, and the chelating tank 805 is provided with two chelating tanks 805 connected in series, and each chelating tank 805 is provided with at least two transverse partitions, and each transverse partition is evenly distributed with through holes.

[0039] The outlet of the chelating tank 805 is connected to the inlet of the second decanter centrifuge 807 through the post-chelating protein delivery pump 806. The inlet pipeline of the second decanter centrifuge 807 is installed with a post-chelating regulating valve FC807 interlocked with the inlet flow. The clear liquid outlet of the second decanter centrifuge 807 is connected to a sewage pipe.

[0040] The protein outlet of the second horizontal screw centrifuge 807 is connected to the second protein buffer tank 808, and the top of the second protein buffer tank 808 is connected to the RO water pipe through the RO water regulating valve FC808. The bottom outlet of the second protein buffer tank 808 is connected to the inlet of the refined protein slurry delivery pump 809.

[0041] The inlet pipe of the sodium carbonate discharge metering pump 813 is inserted into the sodium carbonate tank 812, and the outlet of the sodium carbonate discharge metering pump 813 is also connected to the inlet of the refined protein slurry delivery pump 809, and the rotation speed of the sodium carbonate discharge metering pump 813 is controlled by the pH value of the outlet of the refined protein slurry delivery pump 809.

[0042] The protein slurry from the liquefaction section enters the first horizontal screw centrifuge 801 for further cleaning and separation, and the separated clear liquid enters the sugar water tank 814. Since the clear liquid contains some sugar, it can be used as process water and transported to the mill through the sugar water delivery pump 815 as slurry mixing water, thereby increasing the yield of the syrup.

[0043] The protein from the concentrated phase of the first horizontal screw centrifuge 801 is mixed with a certain proportion of RO water and enters the first protein buffer tank 802. At the same time, citric acid is added in proportion through the citric acid discharge metering pump 811 to chelate heavy metals in the protein. The speed and flow rate of the citric acid discharge metering pump 811 are linked to the pH value sensor at the outlet of the pre-chelation protein delivery pump 803 to control the addition ratio of citric acid and accurately adjust the pH value to 4.

[0044] The protein slurry after adding citric acid is heated indirectly by steam through the heating heat exchanger 804 to increase its temperature. The protein slurry outlet pipe of the heating heat exchanger 804 is installed with a temperature sensor. The hot side inlet of the heating heat exchanger 804 is connected to the steam pipe through the steam regulating valve TC804. The opening of the steam regulating valve TC804 is linked to the protein slurry temperature measured by the temperature sensor. The opening of the steam regulating valve TC804 is adjusted to make the protein slurry outlet temperature reach the set chelating optimal temperature of 75°C.

[0045] After adding citric acid and adjusting the temperature, the protein slurry reaches the optimal heavy metal chelation condition and enters the two-stage chelation tank 805 in series. Each chelation tank 805 is provided with two transverse partitions, and the transverse partitions are evenly distributed with through holes to ensure the relative first-in-first-out of materials. The chelated protein slurry is sent to the second horizontal screw centrifuge 807 for separation through the post-chelation protein delivery pump 806. The clear liquid after separation contains heavy metals and is directly discharged.

[0046] The heavy protein discharged from the concentrated phase of the second horizontal screw centrifuge 807 is mixed with a certain proportion of RO water and then fed into the second protein buffer tank 808. At the same time, sodium carbonate is added in proportion through the sodium carbonate discharge metering pump 813. The frequency of the sodium carbonate discharge metering pump 813 is linked with the pH sensor at the outlet of the refined protein slurry delivery pump 809 to control the sodium carbonate addition ratio to neutralize the protein slurry. After the protein slurry is neutralized, a protein removal sterilization unit is performed.

[0047] like Figure 2 As shown, the protein sterilization unit includes an ejector 901 , a maintenance pipe 902 , a steam filter 903 , a flash tank 904 , a gas-liquid separator 905 , a post-flash transfer pump 906 , a dehydration horizontal screw centrifuge 907 and a wet protein conveyor 908 .

[0048] The main inlet of the ejector 901 is connected to the outlet of the refined protein slurry delivery pump 809 , and the steam inlet of the ejector 901 is connected to the steam pipeline 700 through the ejection steam regulating valve PC901 and the steam filter 903 .

[0049] The outlet of the ejector 901 is connected to the inlet of the maintenance pipe 902, the outlet of the maintenance pipe 902 is connected to the side wall inlet of the flash tank 904, the bottom outlet of the flash tank 904 is connected to the inlet of the dehydration horizontal screw centrifuge 907 through the post-flash delivery pump 906, the inlet of the dehydration horizontal screw centrifuge 907 is installed with a flow meter and a dehydration feed amount regulating valve FC907, and the protein outlet of the dehydration horizontal screw centrifuge 907 is connected to the protein drying unit through the wet protein conveyor 908.

[0050] A defoaming device is provided on the top of the flash tank 904, and the flash steam outlet at the top is connected to the middle inlet of the gas-liquid separator 905, the bottom outlet of the gas-liquid separator 905 is connected to the bottom pipeline of the flash tank 904, and the secondary steam outlet of the gas-liquid separator 905 is connected to the heat source inlet of the triple-effect evaporator of the syrup evaporation and concentration unit.

[0051] The protein slurry after pH adjustment is mixed with steam and heated in the ejector 901. The outlet of the ejector 901 is provided with an ejection temperature sensor TT901. The temperature measured by the ejection temperature sensor TT901 is interlocked with the ejector needle valve TC901 to achieve automatic control. At the same time, an ejection steam regulating valve PC901 and an ejection steam pressure sensor PA901 are installed on the steam pipeline. By controlling the opening of the ejection steam regulating valve PC901, the steam pressure entering the ejector is controlled to maintain stable operation of the ejector 901 and achieve precise control.

[0052] The steam pipe is made of stainless steel to prevent the entry of iron ions, and is equipped with a steam filter 903 to remove impurities in the steam pipe and keep the steam clean.

[0053] The protein slurry after spraying enters the maintenance pipe 902 and is maintained for 10-20 seconds to allow the protein slurry to be quickly sterilized at high temperature. The sterilized protein slurry enters the flash tank 904 for flash cooling. Because bubbles are easily generated in the vacuum state of the protein slurry, a defoaming device is provided on the top of the flash tank 904, and a gas-liquid separator 905 is added to the secondary steam outlet to continue to remove the foam entrained from the secondary steam. The flashed secondary steam enters the triple-effect evaporator of the syrup evaporation and concentration unit as a heat source to realize the utilization of waste heat and reduce the raw steam consumption of the evaporation and concentration unit.

[0054] The protein slurry after flash evaporation cooling is sent to the dehydration horizontal screw centrifuge 907 for separation and dehydration through the post-flash evaporation delivery pump 906. The clear liquid of the dehydration horizontal screw centrifuge 907 is directly discharged, and the heavy protein is transported to the drying section through the wet protein conveyor 908.

[0055] The above description is only the preferred feasible embodiment of the utility model, which shows and describes the basic principle, main features and advantages of the utility model, but does not limit the scope of patent protection of the utility model. The technicians in this industry should understand that the utility model is not limited by the above embodiments. In addition to the above embodiments, the utility model can also have other implementation modes without departing from the spirit and scope of the utility model. The utility model will also have various changes and improvements. All technical solutions formed by equivalent replacement or equivalent transformation fall within the scope of protection required by the utility model. The scope of protection required by the utility model is defined by the attached claims and their equivalents. The technical features not described in the utility model can be achieved by or using existing technologies, which will not be repeated here.

Claims

1. A food-grade rice protein washing, refining and sterilizing device, comprising a first horizontal screw centrifuge (801) connected to a protein slurry outlet of a liquefaction stage, characterized in that: The protein outlet of the first decanter centrifuge (801) is connected to the first protein buffer tank (802), the bottom outlet of the first protein buffer tank (802) is connected to the cold side inlet of the heating heat exchanger (804) through the pre-chelating protein delivery pump (803), the inlet of the pre-chelating protein delivery pump (803) is also connected to the outlet of the citric acid discharge metering pump (811), the cold side outlet of the heating heat exchanger (804) is connected to the inlet of the chelating tank (805), and the chelating tank The outlet of (805) is connected to the inlet of the second decanter centrifuge (807) through the chelated protein delivery pump (806), the protein outlet of the second decanter centrifuge (807) is connected to the second protein buffer tank (808), and the bottom outlet of the second protein buffer tank (808) is connected to the protein sterilization unit through the refined protein slurry delivery pump (809), and the inlet of the refined protein slurry delivery pump (809) is also connected to the outlet of the sodium carbonate discharge metering pump (813).

2. The food-grade rice protein washing, refining and sterilizing device according to claim 1, characterized in that: The tops of the first protein buffer tank (802) and the second protein buffer tank (808) are connected to RO water pipes via RO water regulating valves, respectively.

3. The food-grade rice protein washing, refining and sterilizing device according to claim 1, characterized in that: The clear liquid outlet of the first horizontal screw centrifuge (801) is connected to a sugar water tank (814), and the bottom outlet of the sugar water tank (814) is connected to the mixing water inlet of the mill through a sugar water delivery pump (815).

4. The food-grade rice protein washing, refining and sterilizing device according to claim 1, characterized in that: The chelating tank (805) is provided with two chelating tanks (805) connected in series, each chelating tank (805) is provided with at least two transverse partitions, and each transverse partition is evenly distributed with through holes.

5. The food-grade rice protein washing, refining and sterilizing device according to claim 1, characterized in that: The clear liquid outlet of the second horizontal screw centrifuge (807) is connected to a sewage pipe.

6. The food-grade rice protein washing, refining and sterilizing device according to claim 1, characterized in that: The hot side inlet of the heating heat exchanger (804) is connected to the steam pipeline (700) through a steam regulating valve (TC804), and the opening of the steam regulating valve (TC804) is controlled by the cold side outlet temperature of the heating heat exchanger (804).

7. The food-grade rice protein washing, refining and sterilizing device according to claim 1, characterized in that: The rotation speed of the citric acid discharge metering pump (811) is controlled by the pH value at the outlet of the pre-chelating protein delivery pump (803), and the rotation speed of the sodium carbonate discharge metering pump (813) is controlled by the pH value at the outlet of the refined protein slurry delivery pump (809).

8. The food-grade rice protein washing, refining and sterilizing device according to claim 1, characterized in that: The inlet pipes of the first decanter centrifuge (801) and the second decanter centrifuge (807) are respectively installed with regulating valves interlocked with the inlet flow rates.

9. The food-grade rice protein washing, refining and sterilizing device according to claim 1, characterized in that: The protein sterilization unit comprises an ejector (901), the main inlet of the ejector (901) is connected to the outlet of the refined protein slurry delivery pump (809), the steam inlet of the ejector (901) is connected to the steam pipeline (700) via an ejection steam regulating valve (PC901) and a steam filter (903), the outlet of the ejector (901) is connected to the inlet of a maintenance pipe (902), the outlet of the maintenance pipe (902) is connected to the side wall inlet of a flash tank (904), the bottom outlet of the flash tank (904) is connected to the inlet of a dehydration horizontal screw centrifuge (907) via a post-flash delivery pump (906), and the protein outlet of the dehydration horizontal screw centrifuge (907) is connected to the protein drying unit via a wet protein conveyor (908).

10. The food-grade rice protein washing, refining and sterilizing device according to claim 9, characterized in that: The top of the flash tank (904) is provided with a defoaming device, and the flash steam outlet at the top is connected to the middle inlet of the gas-liquid separator (905), the bottom outlet of the gas-liquid separator (905) is connected to the bottom pipeline of the flash tank (904), and the secondary steam outlet of the gas-liquid separator (905) is connected to the heat source inlet of the triple-effect evaporator of the syrup evaporation and concentration unit.

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