CN106868075B - Protein separation method in starch sugar production - Google Patents
Protein separation method in starch sugar production Download PDFInfo
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- CN106868075B CN106868075B CN201710240220.5A CN201710240220A CN106868075B CN 106868075 B CN106868075 B CN 106868075B CN 201710240220 A CN201710240220 A CN 201710240220A CN 106868075 B CN106868075 B CN 106868075B
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Abstract
The invention discloses a protein separation method in starch sugar production, which is characterized in that a liquefied liquid sprayed at one time is fully liquefied and flocculated by a column type liquefier, and then is separated by a protein separation tank to obtain an overflow liquid and a bottom flow liquefied liquid, the bottom flow liquefied liquid continues the production of starch sugar, the overflow liquid is squeezed to obtain a protein cake and a filtered liquefied liquid, the filtered liquefied liquid returns to the previous procedure for repeated treatment, and the protein cake is processed into a finished product. The invention has simple structure and convenient operation, can improve the yield of protein powder, thereby improving the added value of products, reducing the number of equipment, reducing the dosage of diatomite, reducing the energy consumption and bringing greater economic benefit to enterprises.
Description
Technical Field
The invention belongs to the technical field of starch sugar production, and particularly relates to a protein separation method in starch sugar production.
Background
Starch is hydrolyzed by alpha-amylase to change large molecules into relatively small molecules (dextrin), and protein in the starch is liberated, because the protein in the liquefied liquid is basically soluble, the formed protein is flocculent and has high viscosity. At present, most starch sugar manufacturers adopt a method of not processing liquefied liquid, and then processing and removing the starch sugar by a precoating vacuum filter or a plate and frame filter device after saccharification. Therefore, liquefied liquid cooling equipment (plate heat exchangers and the like) is blocked frequently, the service life of the cooling equipment is shortened, and saccharifying enzyme, filter aids (diatomite, perlite, activated carbon) and the like are consumed more. The production process is also adopted by manufacturers to carry out filter pressing treatment on the liquefied liquid by adopting a plate-and-frame filter press, the protein coming out of the rotary drum filter or the plate-and-frame filter contains a large amount of impurities such as fat, diatomite, ash and the like, and the protein can be sold at low price only along with the impurities according to low added value or after being dried; and because the DE value of the liquefied liquid is not high (generally about 15%), the viscosity of the sugar liquid is high, the filtering is very difficult, the filtering area has to be set large, the investment equipment and the plant area are overlarge, the filtering of the liquefied liquid with 3 ten thousand tons of sugar output per year generally needs 6 to 8 filters with the filtering area of 120 square meters, the occupied area is 90 to 120 square meters, and the popularization of enterprises and the production cost saving are not facilitated. Therefore, how to effectively separate and remove protein in the starch liquefaction liquid becomes a great technical problem which needs to be solved urgently in the starch sugar industry.
The existing starch sugar production process flow is as follows: starch milk → primary spray (105-110 ℃) → column liquefier (laminar flow tube) → secondary spray (125-135 ℃) → column liquefier (laminar flow tube) → saccharification → protein deslagging and filtering → decolorization → ion exchange → evaporation (→ concentration → packaging → finished syrup) → crystallization → drying → packaging → finished product.
Disclosure of Invention
The purpose of the invention is: the protein separation method in starch sugar production is provided, and the protein separation process is added after the primary spraying, so that residues generated in deslagging and filtering of the saccharified protein in the prior art are reduced, rotary drum or plate and frame filter equipment is reduced, the dosage of diatomite is reduced, the starch sugar production cost is reduced, and the yield of protein and the added value of products are improved.
In order to solve the technical problems, the technical scheme of the invention is as follows:
a method for separating protein in starch sugar production comprises the following steps:
a. performing primary injection on the starch milk through an injector to obtain primary injection liquefied liquid;
b. fully liquefying and flocculating the primary injection liquefied liquid by a column type liquefier, conveying the primary injection liquefied liquid to a protein separation tank through a liquid inlet of the protein separation tank for separation, and overflowing the floating liquid on the upper layer out of the protein separation tank to obtain overflow liquid; the lower layer is bottom flow liquefied liquid, enters a secondary spraying procedure through a bottom flow outlet of the protein separation tank, and is sequentially used for producing starch sugar;
c. and filtering the overflow liquid at high temperature to obtain a protein cake and a filtered liquefied liquid, refluxing the filtered liquefied liquid to the primary injection liquefied liquid for continuous treatment, and drying the protein cake to obtain the protein powder.
Preferably, the overflow liquid obtained in the step b is squeezed to obtain a protein cake and a filtered liquefied liquid, the filtered liquefied liquid is refluxed to the primary spray liquefied liquid for continuous treatment, and the protein cake is dried to obtain protein powder. The protein powder can be sold as a commodity.
Preferably, the liquid inlet flow rate of the liquid inlet in the step b is greater than the liquid outlet flow rate of the underflow outlet.
Preferably, in the step b, the primary injection liquefied liquid enters a flow guide pipe arranged in the protein separation tank through a liquid inlet of the protein separation tank through a pipeline, is divided by a flow dividing cone and then enters the tank body, and is layered to obtain an upper floating liquid and a bottom flow liquefied liquid. The floating liquid in the upper layer mainly contains protein and primary spraying liquefied liquid.
Preferably, the side wall of the tank body of the protein separation tank in the step b is respectively provided with a liquid inlet and an overflow port, and the liquid inlet is higher than the overflow port; the bottom of the tank body is provided with a bottom outflow port; the internal vertical hollow honeycomb duct that is provided with of jar, honeycomb duct top opening, the top opening height is higher than the inlet height, and the inlet communicates the top opening of honeycomb duct through the feed liquor pipe, and honeycomb duct lower part opening fixed connection is provided with conical reposition of redundant personnel awl on the support, and the awl point of reposition of redundant personnel awl is put corresponding to the central point of honeycomb duct pipe diameter.
Preferably, the support is fixedly connected to the support rod, two ends of the support rod are fixedly connected to two sides of the inner wall of the tank body, and a distance is reserved between the support rod and the bottom of the tank body.
Preferably, the conical surface of the shunting cone is away from the port edge of the bottom of the guide pipe. The vertical distance is 4-10 cm.
Preferably, the vertical distance between the edge of the lower port of the draft tube and the inner side surface of the bottom of the tank body is 0.2-0.5 m.
Preferably, the draft tube is a cylindrical, elliptic cylindrical or polyhedral draft tube.
Preferably, the support rod is tubular or plate-shaped.
Preferably, the filter pressing equipment is a high-temperature filter or a plate and frame filter.
Preferably, the outer side of the tank body is provided with a heat-insulating layer.
The invention principle is as follows:
the method is mainly applied to the production of corn starch sugar, and the separation of protein in the primary injection liquefied liquid; the method is characterized in that protein can automatically float to the upper layer of liquefied liquid by utilizing the difference of specific gravity, heavy sugar liquid and light protein of protein and sugar liquid, and then the floating liquid containing the protein on the upper layer overflows in an overflow mode; and filtering or squeezing the floating liquid to separate out protein in sugar liquid in starch sugar production.
Due to the adoption of the technical scheme, the invention has the beneficial effects that:
1. in the production of starch sugar and corn starch, the protein separated from the liquefied solution after the technology is used can be directly added into corn protein powder and sold according to the price of the protein powder, and the protein can only be treated as waste in the prior art, so that the added value of the product is improved.
2. The yield of the protein powder in the production process of the corn starch and the starch sugar is improved from about 5.0 percent to about 5.4 percent.
3. The number of equipment is reduced, the equipment consumption is reduced, and energy is saved; calculating according to the annual yield of 6 million tons of crystalline glucose, before using the method, two rotary drum filters with a square meter of 40 or 4 plate-and-frame filters with a filtering area of 100 square meters are needed in the protein residue removal filtering process; after the method is used, 1 rotary drum filter with 40 square meters or 2 plate and frame filters with 100 square meters of filter area are needed in the protein residue removal and filtration process. If the total power of each rotary drum filter of 40 square meters is 75Kw, and the total power of each plate frame filter and the supporting facilities thereof is 23Kw, the power of the equipment is saved by at least 46Kw after the method is used.
4. Because the number of subsequent treatment equipment is reduced, a large amount of building area is not needed, and because the saccharification liquid does not need to be put into a precoating vacuum drum filter, the use amount of filter auxiliary materials such as diatomite, perlite and the like is saved.
In a word, the invention has simple structure and convenient operation, can improve the yield of the protein powder, thereby improving the added value of the product, reducing the number of equipment, reducing the dosage of the diatomite, reducing the energy consumption and bringing greater economic benefit to enterprises.
Drawings
FIG. 1 is a schematic diagram of the structure of a protein separation tank of the present invention;
in the figure, 1-tank body; 2-liquid inlet; 3-an overflow port; 4-a liquid inlet pipe; 5-a flow guide pipe; 6-a scaffold; 7-a spreader cone; 8-a support bar; 9-underflow outlet.
Detailed Description
The invention is further illustrated by the following examples.
The first embodiment is as follows:
the protein separation device in starch sugar production comprises a protein separation tank and a filter pressing device, wherein a liquid inlet 2 and an overflow port 3 are arranged on the side wall of a tank body 1 of the protein separation tank, and the liquid inlet 2 is higher than the overflow port 3; a hollow flow guide pipe 5 is vertically arranged in the tank body, the top end of the flow guide pipe 5 is opened, the top end opening is higher than the liquid inlet 3, the liquid inlet 2 is communicated with the upper end of the flow guide pipe 5 through a liquid inlet pipe 4, the lower end opening of the flow guide pipe 5 is fixedly connected with a bracket 6, the center of the bracket 6 is provided with a conical diversion cone 7, the bracket 6 is fixedly connected to a support rod 8, the support rod 8 keeps a certain distance (0.3m) from the bottom of the tank body, the bottom of the tank body is provided with an underflow outlet 9, and; the filter pressing equipment is a plate and frame filter.
The primary jet liquefied liquid is fully liquefied and flocculated by a column type liquefier and then enters a protein separation tank through a liquid inlet pipe 4 for communicating a liquid inlet 2 with a flow guide pipe 5 at a flow rate of 35 cubic meters per hour, the protein separation tank is made of SUS304, the circular flow guide pipe 5 is arranged inside a tank body 1 of the protein separation tank, the gap between the bottom of the flow guide pipe 5 and the conical surface of a shunting cone is 0.04m, and the distance between the upper part of the flow guide pipe 5 and the top of the protein separation tank is 0.3 m. The exterior of a tank body 1 of the protein separation tank is subjected to heat preservation by rock wool, the diameter of the protein separation tank is 2m, the height of the tank is 5.0m, and the cross section area of a pipeline of the honeycomb duct 5 is 0.05 square meter. Wherein the upper edge of the draft tube 5 in the protein separation tank is higher than the liquid inlet 3, and the height difference is 20 cm. Thus, the primary injection liquefied liquid flows out of the guide pipe 5, is shunted by the shunting cone 7 to generate rotational flow, slowly moves in the tank body 1, and simultaneously sinks the primary injection liquefied liquid and floats protein; finally, the protein forms floccule on the upper layer and enters a plate and frame filter through an overflow port 3; the primary injection liquefied liquid flows out through an underflow outlet 9 at the bottom of the tank body 1, the outflow flow rate of the primary injection liquefied liquid is 33 cubic meters per hour, the primary injection liquefied liquid enters a laminar flow pipe, and then the production process of starch sugar is continued.
The protein on the upper layer has good flocculation effect and is in a sheet shape, then the sheet shape is squeezed by a plate and frame filter, the squeezing pressure is controlled at 0.5Mpa, and most of the solid matters intercepted after squeezing are protein and also contain other small amount of impurities. The solid matters can be directly added into a protein tube bundle dryer in the production process of corn starch, and after being dried, the solid matters can be sold as commercial protein powder, and the color and luster of the commercial protein powder are not different from those of the commercial protein powder. The squeezed liquid is mainly sugar liquid, and is continuously returned to the primary spraying liquefied liquid for circular treatment.
By using the method and the device of the embodiment, 65% of protein in the primary spray liquefied liquid is separated, so that the yield of protein powder in starch sugar produced by processing the whole corn is improved by 0.28%.
Example two:
the primary jet liquefied liquid is fully liquefied and flocculated by a column type liquefier and then enters a protein separation tank through a liquid inlet pipe 4 for communicating a liquid inlet 2 with a flow guide pipe 5 at a flow rate of 40 cubic meters per hour, the protein separation tank is made of SUS304, the circular flow guide pipe 5 is arranged inside a tank body 1 of the protein separation tank, the gap between the bottom of the flow guide pipe 5 and the conical surface of a shunting cone is 0.05m, and the distance between the upper part of the flow guide pipe 5 and the top of the protein separation tank is 0.3 m. The exterior of a tank body 1 of the protein separation tank is subjected to heat preservation by polyurethane, the diameter of the protein separation tank is 3m, the height of the tank is 6.5m, and the cross section area of a pipeline of the honeycomb duct 5 is 0.07 square meter. Wherein the upper edge of the draft tube 5 in the protein separation tank is higher than the liquid inlet 3, and the height difference is 20 cm. Thus, the primary injection liquefied liquid flows out of the guide pipe 5, is shunted by the shunting cone 7 to generate rotational flow, slowly moves in the tank body 1, and simultaneously sinks the primary injection liquefied liquid and floats protein; finally, the protein forms floccule on the upper layer and enters a plate and frame filter through an overflow port 3; the primary injection liquefied liquid flows out through an underflow outlet 9 at the bottom of the tank body 1, the outflow flow rate is 38 cubic meters per hour, the primary injection liquefied liquid enters a laminar flow pipe, and then the production process of the starch sugar is continued.
The protein on the upper layer has good flocculation effect and is in a sheet shape, then the sheet shape is squeezed by a plate and frame filter, the squeezing pressure is controlled at 0.5Mpa, and most of the solid matters intercepted after squeezing are protein and also contain other small amount of impurities. The solid matters can be directly added into a protein tube bundle dryer in the production process of corn starch, and after being dried, the solid matters can be sold as commercial protein powder, and the color and luster of the commercial protein powder are not different from those of the commercial protein powder. The squeezed liquid is mainly sugar liquid, and is continuously returned to the primary spraying liquefied liquid for circular treatment.
By using the method and the device of the embodiment, 68% of protein in the primary spray liquefied liquid is separated, so that the yield of protein powder in starch sugar production by whole corn processing is improved by 0.30%.
Example three:
the primary jet liquefied liquid is fully liquefied and flocculated by a column type liquefier and then enters a protein separation tank through a liquid inlet pipe 4 for communicating a liquid inlet 2 with a flow guide pipe 5 at a flow rate of 42 cubic meters per hour, the protein separation tank is made of SUS304, the tank body 1 of the protein separation tank is internally provided with the circular flow guide pipe 5, the gap between the bottom of the flow guide pipe 5 and the conical surface of a shunting cone is 0.05m, and the upper part of the flow guide pipe 5 is 0.3m away from the top of the protein separation tank. The exterior of a tank body 1 of the protein separation tank is subjected to heat preservation by polyurethane, the diameter of the protein separation tank is 3.5m, the height of the tank is 7.0m, and the cross-sectional area of a pipeline of the honeycomb duct 5 is 0.07 square meter. Wherein the upper edge of the draft tube 5 in the protein separation tank is higher than the liquid inlet 3, and the height difference is 20 cm. Thus, the primary injection liquefied liquid flows out of the guide pipe 5, is shunted by the shunting cone 7 to generate rotational flow, slowly moves in the tank body 1, and simultaneously sinks the primary injection liquefied liquid and floats protein; finally, the protein forms floccule on the upper layer and enters a plate and frame filter through an overflow port 3; the primary injection liquefied liquid flows out through an underflow outlet 9 at the bottom of the tank body 1, the outflow flow rate of the primary injection liquefied liquid is 40 cubic meters per hour, the primary injection liquefied liquid enters a laminar flow pipe, and then the production process of starch sugar is continued.
The protein on the upper layer has good flocculation effect and is flaky, then the upper layer is filtered by a high-temperature filter, and most of the solid matters intercepted after the filtration are protein and also contain other small amount of impurities. The solid matters can be directly added into a protein tube bundle dryer in the production process of corn starch, and after being dried, the solid matters can be sold as commercial protein powder, and the color and luster of the commercial protein powder are not different from those of the commercial protein powder. The squeezed liquid is mainly sugar liquid, and is continuously returned to the primary spraying liquefied liquid for circular treatment.
By using the method and the device of the embodiment, 70% of protein in the primary spray liquefied liquid is separated, so that the yield of protein powder in starch sugar produced by processing the whole corn is improved by 0.31%.
Example four:
the primary jet liquefied liquid is fully liquefied and flocculated by a column type liquefier and then enters a protein separation tank through a liquid inlet pipe 4 for communicating a liquid inlet 2 with a flow guide pipe 5 at a flow rate of 45 cubic meters per hour, the protein separation tank is made of SUS304, the tank body 1 of the protein separation tank is internally provided with the circular flow guide pipe 5, the gap between the bottom of the flow guide pipe 5 and the conical surface of a shunting cone is 0.08m, and the upper part of the flow guide pipe 5 is 0.3m away from the top of the protein separation tank. The exterior of a tank body 1 of the protein separation tank is subjected to heat preservation by polyurethane, the diameter of the protein separation tank is 4.0m, the height of the tank is 8.0m, and the cross-sectional area of a pipeline of the honeycomb duct 5 is 0.08 square meter. Wherein the upper edge of the draft tube 5 in the protein separation tank is higher than the liquid inlet 3, and the height difference is 20 cm. Thus, the primary injection liquefied liquid flows out of the guide pipe 5, is shunted by the shunting cone 7 to generate rotational flow, slowly moves in the tank body 1, and simultaneously sinks the primary injection liquefied liquid and floats protein; finally, the protein forms floccule on the upper layer and enters a plate and frame filter through an overflow port 3; the primary injection liquefied liquid flows out through the bottom flow outlet 9 at the bottom of the tank body 1, the outflow flow rate is 43 cubic meters per hour, the primary injection liquefied liquid enters a laminar flow pipe, and then the production process of starch sugar is continued.
The protein on the upper layer has good flocculation effect and is flaky, then the upper layer is filtered by a high-temperature filter, and most of the solid matters intercepted after the filtration are protein and also contain other small amount of impurities. The solid matters can be directly added into a protein tube bundle dryer in the production process of corn starch, and after being dried, the solid matters can be sold as commercial protein powder, and the color and luster of the commercial protein powder are not different from those of the commercial protein powder. The squeezed liquid is mainly sugar liquid, and is continuously returned to the primary spraying liquefied liquid for circular treatment.
By using the method and the device of the embodiment, 72% of protein in the primary spray liquefied liquid is separated, so that the yield of protein powder in starch sugar production by whole corn processing is improved by 0.32%.
Example five:
the primary jet liquefied liquid is fully liquefied and flocculated by a column type liquefier and then enters a protein separation tank through a liquid inlet pipe 4 for communicating a liquid inlet 2 with a flow guide pipe 5 at a flow rate of 45 cubic meters per hour, the protein separation tank is made of SUS304, the tank body 1 of the protein separation tank is internally provided with the circular flow guide pipe 5, the gap between the bottom of the flow guide pipe 5 and the conical surface of a shunting cone is 0.08m, and the upper part of the flow guide pipe 5 is 0.3m away from the top of the protein separation tank. The exterior of a tank body 1 of the protein separation tank is subjected to heat preservation by polyurethane, the diameter of the protein separation tank is 4.5m, the height of the tank is 8.5m, and the cross-sectional area of a pipeline of the honeycomb duct 5 is 0.08 square meter. Wherein the upper edge of the draft tube 5 in the protein separation tank is higher than the liquid inlet 3, and the height difference is 20 cm. Thus, the primary injection liquefied liquid flows out of the guide pipe 5, is shunted by the shunting cone 7 to generate rotational flow, slowly moves in the tank body 1, and simultaneously sinks the primary injection liquefied liquid and floats protein; finally, the protein forms floccule on the upper layer and enters a plate and frame filter through an overflow port 3; the primary injection liquefied liquid flows out through the bottom flow outlet 9 at the bottom of the tank body 1, the outflow flow rate is 43 cubic meters per hour, the primary injection liquefied liquid enters a laminar flow pipe, and then the production process of starch sugar is continued.
The protein on the upper layer has good flocculation effect and is in a sheet shape, then the sheet shape is squeezed by a plate and frame filter, the squeezing pressure is controlled at 0.5Mpa, and most of the solid matters intercepted after squeezing are protein and also contain other small amount of impurities. The solid matters can be directly added into a protein tube bundle dryer in the production process of corn starch, and after being dried, the solid matters can be sold as commercial protein powder, and the color and luster of the commercial protein powder are not different from those of the commercial protein powder. The squeezed liquid is mainly sugar liquid, and is continuously returned to the primary spraying liquefied liquid for circular treatment.
By using the method and the device of the embodiment, 75% of protein in the primary spray liquefied liquid is separated, so that the yield of protein powder in starch sugar production by whole corn processing is improved by 0.32%.
Example six:
the primary jet liquefied liquid is fully liquefied and flocculated by a column type liquefier and then enters a protein separation tank through a liquid inlet pipe 4 for communicating a liquid inlet 2 with a flow guide pipe 5 at a flow rate of 48 cubic meters per hour, the protein separation tank is made of SUS304, the tank body 1 of the protein separation tank is internally provided with the circular flow guide pipe 5, the gap between the bottom of the flow guide pipe 5 and the conical surface of a shunting cone is 0.10m, and the upper part of the flow guide pipe 5 and the top of the protein separation tank are 0.3m apart. The exterior of a tank body 1 of the protein separation tank is subjected to heat preservation by polyurethane, the diameter of the protein separation tank is 5.0m, the height of the tank is 10.0m, and the cross-sectional area of a pipeline of the honeycomb duct 5 is 0.10 square meter. Wherein the upper edge of the draft tube 5 in the protein separation tank is higher than the liquid inlet 3, and the height difference is 20 cm. Thus, the primary injection liquefied liquid flows out of the guide pipe 5, is shunted by the shunting cone 7 to generate rotational flow, slowly moves in the tank body 1, and simultaneously sinks the primary injection liquefied liquid and floats protein; finally, the protein forms floccule on the upper layer and enters a plate and frame filter through an overflow port 3; the primary injection liquefied liquid flows out through an underflow outlet 9 at the bottom of the tank body 1, the outflow flow rate of the primary injection liquefied liquid is 45 cubic meters per hour, the primary injection liquefied liquid enters a laminar flow pipe, and then the production process of starch sugar is continued.
The protein on the upper layer has good flocculation effect and is flaky, then the upper layer is filtered by a high-temperature filter, and most of the solid matters intercepted after the filtration are protein and also contain other small amount of impurities. The solid matters can be directly added into a protein tube bundle dryer in the production process of corn starch, and after being dried, the solid matters can be sold as commercial protein powder, and the color and luster of the commercial protein powder are not different from those of the commercial protein powder. The squeezed liquid is mainly sugar liquid, and is continuously returned to the primary spraying liquefied liquid for circular treatment.
By using the method and the device of the embodiment, 77% of protein in the primary spray liquefied liquid is separated, so that the yield of protein powder in starch sugar production by whole corn processing is improved by 0.33%.
Example seven:
the primary jet liquefied liquid is fully liquefied and flocculated by a column type liquefier and then enters a protein separation tank through a liquid inlet pipe 4 for communicating a liquid inlet 2 with a flow guide pipe 5 at a flow rate of 48 cubic meters per hour, the protein separation tank is made of SUS304, the tank body 1 of the protein separation tank is internally provided with the circular flow guide pipe 5, the gap between the bottom of the flow guide pipe 5 and the conical surface of a shunting cone is 0.10m, and the upper part of the flow guide pipe 5 and the top of the protein separation tank are 0.3m apart. The exterior of a tank body 1 of the protein separation tank is subjected to heat preservation by polyurethane, the diameter of the protein separation tank is 5.5m, the height of the tank is 11.0m, and the cross-sectional area of a pipeline of the honeycomb duct 5 is 0.10 square meter. Wherein the upper edge of the draft tube 5 in the protein separation tank is higher than the liquid inlet 3, and the height difference is 20 cm. Thus, the primary injection liquefied liquid flows out of the guide pipe 5, is shunted by the shunting cone 7 to generate rotational flow, slowly moves in the tank body 1, and simultaneously sinks the primary injection liquefied liquid and floats protein; finally, the protein forms floccule on the upper layer and enters a plate and frame filter through an overflow port 3; the primary injection liquefied liquid flows out through an underflow outlet 9 at the bottom of the tank body 1, the outflow flow rate of the primary injection liquefied liquid is 45 cubic meters per hour, the primary injection liquefied liquid enters a laminar flow pipe, and then the production process of starch sugar is continued.
The protein on the upper layer has good flocculation effect and is in a sheet shape, then the sheet shape is squeezed by a plate and frame filter, the squeezing pressure is controlled at 0.5Mpa, and most of the solid matters intercepted after squeezing are protein and also contain other small amount of impurities. The solid matters can be directly added into a protein tube bundle dryer in the production process of corn starch, and after being dried, the solid matters can be sold as commercial protein powder, and the color and luster of the commercial protein powder are not different from those of the commercial protein powder. The squeezed liquid is mainly sugar liquid, and is continuously returned to the primary spraying liquefied liquid for circular treatment.
By using the method and the device of the embodiment, 79 percent of protein in the primary spray liquefied liquid is separated, so that the yield of protein powder in starch sugar produced by processing the whole corn is improved by 0.34 percent.
Example eight:
the primary jet liquefied liquid is fully liquefied and flocculated by a column type liquefier and then enters a protein separation tank through a liquid inlet pipe 4 for communicating a liquid inlet 2 with a flow guide pipe 5 at a flow rate of 50 cubic meters per hour, the protein separation tank is made of SUS304, the tank body 1 of the protein separation tank is internally provided with the circular flow guide pipe 5, the gap between the bottom of the flow guide pipe 5 and the conical surface of a shunting cone is 0.10m, and the upper part of the flow guide pipe 5 and the top of the protein separation tank are 0.3m apart. The exterior of a tank body 1 of the protein separation tank is subjected to heat preservation by polyurethane, the diameter of the protein separation tank is 6.0m, the height of the tank is 12.0m, and the cross-sectional area of a pipeline of the honeycomb duct 5 is 0.10 square meter. Wherein the upper edge of the draft tube 5 in the protein separation tank is higher than the liquid inlet 3, and the height difference is 20 cm. Thus, the primary injection liquefied liquid flows out of the guide pipe 5, is shunted by the shunting cone 7 to generate rotational flow, slowly moves in the tank body 1, and simultaneously sinks the primary injection liquefied liquid and floats protein; finally, the protein forms floccule on the upper layer and enters a plate and frame filter through an overflow port 3; the primary injection liquefied liquid flows out through an underflow outlet 9 at the bottom of the tank body 1, the outflow flow rate of the primary injection liquefied liquid is 48 cubic meters per hour, the primary injection liquefied liquid enters a laminar flow pipe, and then the production process of starch sugar is continued.
The protein on the upper layer has good flocculation effect and is in a sheet shape, then the sheet shape is squeezed by a plate and frame filter, the squeezing pressure is controlled at 0.5Mpa, and most of the solid matters intercepted after squeezing are protein and also contain other small amount of impurities. The solid matters can be directly added into a protein tube bundle dryer in the production process of corn starch, and after being dried, the solid matters can be sold as commercial protein powder, and the color and luster of the commercial protein powder are not different from those of the commercial protein powder. The squeezed liquid is mainly sugar liquid, and is continuously returned to the primary spraying liquefied liquid for circular treatment.
By using the method and the device of the embodiment, 76% of protein in the primary spray liquefied liquid is separated, so that the yield of protein powder in starch sugar production by whole corn processing is improved by 0.33%.
It should be understood that these examples are for illustrative purposes only and are not intended to limit the scope of the present invention. Further, it should be understood that various changes or modifications of the present invention may be made by those skilled in the art after reading the teaching of the present invention, and such equivalents may fall within the scope of the present invention as defined in the appended claims.
Claims (8)
1. A method for separating protein in starch sugar production is characterized in that: the method comprises the following steps:
a. performing primary injection on the starch milk through an injector to obtain primary injection liquefied liquid;
b. b, fully liquefying and flocculating the primary injection liquefied liquid obtained in the step a by using a column type liquefier, conveying the primary injection liquefied liquid to a protein separation tank through a liquid inlet of the protein separation tank for separation, and overflowing the floating liquid on the upper layer out of the protein separation tank to obtain overflow liquid; the lower layer is bottom flow liquefied liquid, enters a secondary spraying procedure through a bottom flow outlet of the protein separation tank, and is sequentially used for producing starch sugar;
a liquid inlet and an overflow port are respectively arranged on the side wall of the tank body of the protein separation tank, and the liquid inlet is higher than the overflow port; a bottom outflow port is arranged at the bottom of the tank body; a hollow flow guide pipe is vertically arranged in the tank body, the top end of the flow guide pipe is provided with an opening, the height of the opening at the top end is higher than that of the liquid inlet, the liquid inlet is communicated with the opening at the top end of the flow guide pipe through a liquid inlet pipe, the opening at the lower part of the flow guide pipe is fixedly connected to a support, a conical shunting cone is arranged on the support, and the cone tip of the shunting cone corresponds to the central position of the pipe diameter of the flow guide pipe;
c. and c, filtering the overflow liquid obtained in the step b at high temperature to obtain a protein cake and a filtered liquefied liquid, refluxing the filtered liquefied liquid to the primary injection liquefied liquid for continuous treatment, and drying the protein cake to obtain protein powder.
2. The method for separating proteins in the production of starch sugar according to claim 1, wherein: and the liquid inlet flow of the liquid inlet in the step b is larger than the liquid outlet flow of the underflow outlet.
3. The method for separating proteins in the production of starch sugar according to claim 1, wherein: and c, in the step b, the primary injection liquefied liquid enters a flow guide pipe arranged in the protein separation tank through a liquid inlet of the protein separation tank through a pipeline, is divided by a splitter cone and then enters the tank body, and is layered to obtain an upper floating liquid and a bottom flow liquefied liquid.
4. The method for separating proteins in the production of starch sugar according to claim 1, wherein: the support is fixedly connected to the supporting rod, two ends of the supporting rod are fixedly connected to two sides of the inner wall of the tank body, and a distance is reserved between the supporting rod and the bottom of the tank body.
5. The method for separating proteins in the production of starch sugar according to claim 1, wherein: the cone tip of the shunting cone corresponds to the central position of the pipe diameter of the flow guide pipe, and the vertical distance between the cone surface of the shunting cone and the end opening edge of the bottom of the flow guide pipe is 4-10 cm.
6. The method for separating proteins in the production of starch sugar according to claim 1, wherein: the vertical distance between the lower port edge of the flow guide pipe and the inner side surface of the bottom of the tank body is 0.2-0.5 m.
7. The method for separating proteins in the production of starch sugar according to claim 1, wherein: the honeycomb duct is a cylindrical, elliptic cylindrical or polyhedral honeycomb duct.
8. The method for separating proteins in the production of starch sugar according to claim 1, wherein: and a heat insulation layer is arranged on the outer side of the tank body.
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| CN109517861B (en) * | 2018-11-19 | 2021-05-04 | 山东盛泰生物科技有限公司 | Protein separation method and device in starch sugar production |
| CN111807592B (en) * | 2020-07-17 | 2022-04-15 | 河北兰升生物科技有限公司 | Continuous liquid separation device and organic solvent separation method using same |
| CN114292966A (en) * | 2021-12-23 | 2022-04-08 | 巴彦淖尔华恒生物科技有限公司 | Separation method and application of flocculation protein in starch sugar solution |
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| CN101126109A (en) * | 2007-09-25 | 2008-02-20 | 上海融氏生物科技有限公司 | Production technique for corn starch sugar |
| CN201325937Y (en) * | 2008-12-16 | 2009-10-14 | 山东华义玉米科技有限公司 | Protein recovery device for protein and starch separation section in the production of corn starch |
| CN102516354A (en) * | 2011-11-17 | 2012-06-27 | 玉锋实业集团有限公司 | Separation method and equipment of protein from starch sugar liquefied solution |
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| CN104418933A (en) * | 2013-09-06 | 2015-03-18 | 西安司坤电子科技有限公司 | Protein recycling device in starch sugar production process |
| CN105218622A (en) * | 2014-11-17 | 2016-01-06 | 山东临大教育科技有限公司 | The method of rice cold induced proteins powder and β-amylose is prepared in a kind of coproduction of cracking rice |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101126109A (en) * | 2007-09-25 | 2008-02-20 | 上海融氏生物科技有限公司 | Production technique for corn starch sugar |
| CN201325937Y (en) * | 2008-12-16 | 2009-10-14 | 山东华义玉米科技有限公司 | Protein recovery device for protein and starch separation section in the production of corn starch |
| CN102516354A (en) * | 2011-11-17 | 2012-06-27 | 玉锋实业集团有限公司 | Separation method and equipment of protein from starch sugar liquefied solution |
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