CN106868075A - Method for protein isolation in a kind of starch sugar production - Google Patents
Method for protein isolation in a kind of starch sugar production Download PDFInfo
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- CN106868075A CN106868075A CN201710240220.5A CN201710240220A CN106868075A CN 106868075 A CN106868075 A CN 106868075A CN 201710240220 A CN201710240220 A CN 201710240220A CN 106868075 A CN106868075 A CN 106868075A
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P19/00—Preparation of compounds containing saccharide radicals
- C12P19/14—Preparation of compounds containing saccharide radicals produced by the action of a carbohydrase (EC 3.2.x), e.g. by alpha-amylase, e.g. by cellulase, hemicellulase
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07K—PEPTIDES
- C07K1/00—General methods for the preparation of peptides, i.e. processes for the organic chemical preparation of peptides or proteins of any length
- C07K1/14—Extraction; Separation; Purification
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- C12P19/00—Preparation of compounds containing saccharide radicals
- C12P19/04—Polysaccharides, i.e. compounds containing more than five saccharide radicals attached to each other by glycosidic bonds
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Abstract
The invention discloses method for protein isolation in a kind of production of starch sugar, by the liquefier that will once spray after pillar liquefier fully liquefies flocculation, separated by Protein Separation tank again, obtain overflowing liquid and underflow liquefier, underflow liquefier continues the production of starch sugar, overflowing liquid obtains liquefier after meringue and filter after squeezing, and liquefier returns to preceding operation and repeats to process after filter, meringue processed finished products.It is simple structure of the invention, easy to operate, the yield of albumen powder can be improved, so as to improve value-added content of product, and number of devices is reduced, diatomite consumption is reduced, energy consumption is reduced, bring larger economic benefit to enterprise.
Description
Technical field
The invention belongs to starch sugar production technical field, specifically, Separation of Proteins in being related to a kind of starch sugar to produce
Method.
Background technology
Starch to be hydrolyzed in the presence of AMS and become relatively small molecule (dextrin) by macromolecular, in starch
Albumen will separate out because the albumen in liquefier is substantially soluble, into cotton-shaped, viscosity is also very for the albumen of formation
Greatly.At present, the way that most of starch sugar manufacturer is not processed using liquefier, to saccharification after again by precoated shet vacuum mistake
The treatment of the filter plant such as filter or sheet frame is removed.Liquefier cooling system (plate type heat exchanger etc.) is so not only frequently occluded, is subtracted
Few cooling system life-span, but also consume carbohydrase more, many consumption of filter auxiliary agents (diatomite, perlite, activated carbon) etc..Also have
Producer carries out press filtration treatment using plate and frame filter press to liquefier, using this production technology, from rotary drum filter or sheet frame
Significant quantities of fat is contained in filter albumen the inside out, and diatomite and ash grade impurity, and albumen can only be with these impurity together
Outer sell or undersell after being dried according to low value-added；And because liquefier DE values are not high (left typically 15%
It is right), liquid glucose viscosity is big, filters extremely difficult, it has to filter area set it is very big, used device and plant area are excessive,
The general liquefier filtering for producing 30000 tons of candy outputs per year needs 120 square metres of filters needs 6 to 8 of filter area, takes face
90 to 120 square metres of product, is unfavorable for the popularization of enterprise and saves production cost.Therefore, how liquefied starch is efficiently solved
Middle Protein Separation removal, the significant technology issues as starch sugar industry urgent need to resolve.
The existing starch sugar technological process of production：Starch milk → once spray (105~110 DEG C) → pillar liquefier (laminar flow
Pipe) → secondary injection (125~135 DEG C) → pillar liquefier (laminar flow pipe) → saccharification → albumen deslagging filtering → decolouring → from friendship
→ evaporation (→ concentration → packaging → finished product syrup) → crystallization → drying → packaging → finished product.
The content of the invention
The purpose of the present invention is：Method for protein isolation, the method are because once spraying in providing a kind of starch sugar production
The operation of Separation of Proteins is just with the addition of after penetrating, so that the residue after being saccharified in the prior art during albumen deslagging filtering subtracts
It is few, rotary drum or plate-frame filtering machine equipment are reduced so as to reach, the effect of diatomite consumption is reduced, and reduce starch sugar production
Cost, improves the yield and value-added content of product of protein.
In order to solve the above technical problems, the technical scheme is that：
Method for protein isolation in a kind of starch sugar production, comprises the following steps：
A. starch milk is once sprayed through injector, is once sprayed liquefier；
B. will once spray liquefier through pillar liquefier fully liquefy flocculation after, the inlet by Protein Separation tank is defeated
It is sent to Protein Separation tank to be separated, the flotation fluid overflow on upper strata is gone out into Protein Separation tank, obtains overflowing liquid；Lower floor is underflow liquid
Change liquid, secondary injection operation is entered into through the underflow outlet of Protein Separation tank, the production of starch sugar is carried out successively；
C. overflowing liquid is carried out into high temperature filtration, obtains liquefier after meringue and filter, liquefier after filter is back to once
Injection liquefier is continued with, and meringue drying and processing obtains albumen powder.
Preferably, the overflowing liquid that described step b is obtained carries out squeezing treatment, obtains liquefier after meringue and filter, will
Liquefier is back to once injection liquefier and continues with after filter, and meringue drying and processing obtains albumen powder.Albumen powder can be made
It is commodity selling.
Preferably, the flow quantity that enters of inlet goes out flow quantity more than underflow outlet in described step b.
Preferably, in described step b liquefier is once sprayed to be entered into by pipeline through the inlet of Protein Separation tank
The mozzle inside the Protein Separation tank is arranged on, then is entered in tank body after spreader shunting, be layered, obtain upper strata
Flotation fluid and bottom underflow liquefier.Protein is mainly contained in the flotation fluid on upper strata and liquefier is once sprayed.
Preferably, inlet and overfall are respectively arranged with the Protein Separation tank side wall in described step b, are entered
Liquid mouthful position is higher than overfall；The bottom of tank body is provided with underflow outlet；Hollow mozzle, water conservancy diversion are vertically provided with tank body
Pipe top end opening, top end opening is highly higher than feed liquor open height, and inlet is communicated to the top end opening of mozzle by feed tube,
Mozzle lower openings are fixedly attached on support, and the spreader of cone shape, the cone correspondence of spreader are provided with support
In the center of mozzle caliber.
Preferably, described support is fixedly attached on support bar, and support bar two ends are fixedly attached to inner tank wall both sides,
Distance is provided between support bar and tank base.
Preferably, the conical surface of described spreader is provided with distance with mozzle bottom port opening's edge.Its vertical range is 4
~10 centimetres.
Preferably, described mozzle lower port opening's edge is 0.2~0.5 with the vertical range of tank base medial surface
Rice.
Preferably, described mozzle is cylindric, elliptic cylindrical shape or polyhedral mozzle.
Preferably, described support bar is tubulose or tabular.
Preferably, described filtering equipment is high temperature filtration machine or flame filter press.
Preferably, described tank body outside is provided with heat-insulation layer.
Inventive principle：
This method is applied primarily in corn starch sugar production, once sprays the separation of protein in liquefier；Using egg
White matter is different with the proportion of liquid glucose, liquid glucose weight, albumen light weight, and protein can automatically float to the upper strata of liquefier, then will be upper
Flotation fluid of the layer containing protein is overflowed by way of overflow；Flotation fluid is filtered or squeezing treatment again, i.e.,
Separation of Proteins during can starch sugar be produced in liquid glucose is out.
By adopting the above-described technical solution, the beneficial effects of the invention are as follows：
1st, in starch sugar and production of corn starch, the albumen after using the technology by being separated after liquefier
Matter can be added directly into corn protein powder, sold according to albumen powder price, can only be carried as waste disposal in the prior art
High product added value.
2nd, the albumen powder yield in cornstarch and starch sugar production process is improve, by original 5.0% or so, is carried
Up to 5.4% or so.
3rd, number of devices is reduced, equipment consumption is reduced, the energy has been saved；According to 60,000 tons of crystal glucose meters of annual output
Calculate, before using the method, albumen deslagging filtering operation needs to use two 4 mistakes of rotary drum filter or use of 40 ㎡
Filtering surface accumulates the flame filter press of 100 ㎡；Using after the method, albumen deslagging filtering operation needs to use turning for 1 40 ㎡
Drum filter uses 2 flame filter presses of the ㎡ of filter area 100.If every rotary drum filter general power of 40 ㎡
75Kw, every flame filter press and its auxiliary facility general power 23Kw, after the method, equipment dynamic saves at least 46Kw.
4th, because reducing subsequent processing device quantity, therefore also without a large amount of construction areas of occupancy, and because sugar
Changing liquid need not come into operation precoated shet vacuum-type drum filter, so as to save the usage amount that diatomite and perlite etc. filter auxiliary material.
In a word, simple structure of the invention, easy to operate, can improve the yield of albumen powder, so as to improve the attached of product
It is value added, and number of devices is reduced, diatomite consumption is reduced, energy consumption is reduced, bring larger economic benefit to enterprise.
Brief description of the drawings
Fig. 1 is the structural representation of Protein Separation tank of the present invention；
In figure, 1- tank bodies；2- inlets；3- overfalls；4- feed tubes；5- mozzles；6- supports；7- spreaders；8- branch
Strut；9- underflow outlets.
Specific embodiment
With reference to embodiment, the present invention is expanded on further.
Embodiment one：
Separation of Proteins device in starch sugar production of the invention, including Protein Separation tank and filtering equipment, Protein Separation
Inlet 2 and overfall 3 are provided with the side wall of tank body 1 of tank, the position of inlet 2 is higher than overfall 3；It is vertically provided with tank body
Hollow mozzle 5, the top end opening of mozzle 5, top end opening is higher than inlet 3, and inlet 2 is communicated to by feed tube 4 and led
The upper end of flow tube 5, the lower port of mozzle 5 is fixedly connected with support 6, and support 6 is provided centrally with the spreader 7 of cone shape,
Support 6 is fixedly attached on support bar 8, and support bar 8 maintains a certain distance (0.3m) with tank base, and tank base is provided with
Underflow outlet 9, underflow outlet 9 is connected to filtering equipment by pipeline；Filtering equipment is flame filter press.
Liquefier will be once sprayed to pass through with flow as 35 cubes ms/h after pillar liquefier fully liquefies flocculation
The feed tube 4 of connection inlet 2 and mozzle 5 enters into Protein Separation tank, and the material of Protein Separation tank is SUS304, albumen point
Circular housing 5 is provided that inside the tank body 1 of tank, the gap between the bottom of mozzle 5 and the spreader conical surface is 0.04m's
There is the distance of 0.3m at the top of distance, the top of mozzle 5 and affiliated Protein Separation tank.The outside of tank body 1 of Protein Separation tank is passed through
Rock wool heat-preservation, a diameter of 2m of Protein Separation tank, tank 5.0m high, the affiliated pipeline section product of mozzle 5 is in 0.05 ㎡.Wherein egg
Along inlet 3 is higher by white knockout drum inner guiding pipe 5, its difference in height is 20cm.So, liquefier from mozzle is once sprayed
Flowed out in 5, by the shunting of spreader 7, produce eddy flow, slowly moved in tank body 1, while once will spray under liquefier
Heavy, protein floats；Final protein matter forms floccule on upper strata, and flame filter press is entered into by overfall 3；Once spray
Liquefier is flowed out by the underflow outlet 9 of the bottom of tank body 1, and the flow of its outflow is 33 cubes ms/h, enters into laminar flow pipe,
Then proceed to the production process of starch sugar.
The albumen flocculating effect on upper strata is good, and sheet is presented, and is then squeezed by flame filter press again, and squeeze pressure control exists
0.5Mpa, the solid content major part by retention after squeezing is protein, also contains other a small amount of impurity.These solid contents can be with
The albumen pipe bundle drier during production of corn starch is added directly into, by after drying, being gone out as commodity egg white powder
Sell, its color and luster and albumen powder indifference.Liquid after squeezing is mainly liquid glucose, continues back in once injection liquefier, follows
Ring treatment.
Using the method and apparatus of the present embodiment, will once 65% Separation of Proteins be out in injection liquefier so that
The yield of the albumen powder in whole corn processing production starch sugar improves 0.28%.
Embodiment two：
Liquefier will be once sprayed to pass through with flow as 40 cubes ms/h after pillar liquefier fully liquefies flocculation
The feed tube 4 of connection inlet 2 and mozzle 5 enters into Protein Separation tank, and the material of Protein Separation tank is SUS304, albumen point
Circular housing 5 is provided that inside the tank body 1 of tank, the gap between the bottom of mozzle 5 and the spreader conical surface is 0.05m's
There is the distance of 0.3m at the top of distance, the top of mozzle 5 and affiliated Protein Separation tank.The outside of tank body 1 of Protein Separation tank is passed through
Polyurethane heat-insulation, a diameter of 3m of Protein Separation tank, tank 6.5m high, the affiliated pipeline section product of mozzle 5 is in 0.07 ㎡.Wherein
Along inlet 3 is higher by Protein Separation tank inner guiding pipe 5, its difference in height is 20cm.So, liquefier from water conservancy diversion is once sprayed
Flowed out in pipe 5, by the shunting of spreader 7, produce eddy flow, slowly moved in tank body 1, while once will spray under liquefier
Heavy, protein floats；Final protein matter forms floccule on upper strata, and flame filter press is entered into by overfall 3；Once spray
Liquefier is flowed out by the underflow outlet 9 of the bottom of tank body 1, and the flow of its outflow is 38 cubes ms/h, enters into laminar flow pipe,
Then proceed to the production process of starch sugar.
The albumen flocculating effect on upper strata is good, and sheet is presented, and is then squeezed by flame filter press again, and squeeze pressure control exists
0.5Mpa, the solid content major part by retention after squeezing is protein, also contains other a small amount of impurity.These solid contents can be with
The albumen pipe bundle drier during production of corn starch is added directly into, by after drying, being gone out as commodity egg white powder
Sell, its color and luster and albumen powder indifference.Liquid after squeezing is mainly liquid glucose, continues back in once injection liquefier, follows
Ring treatment.
Using the method and apparatus of the present embodiment, will once 68% Separation of Proteins be out in injection liquefier so that
The yield of the albumen powder in whole corn processing production starch sugar improves 0.30%.
Embodiment three：
Liquefier will be once sprayed to pass through with flow as 42 cubes ms/h after pillar liquefier fully liquefies flocculation
The feed tube 4 of connection inlet 2 and mozzle 5 enters into Protein Separation tank, and the material of Protein Separation tank is SUS304, albumen point
Circular housing 5 is provided that inside the tank body 1 of tank, the gap between the bottom of mozzle 5 and the spreader conical surface is 0.05m's
There is the distance of 0.3m at the top of distance, the top of mozzle 5 and affiliated Protein Separation tank.The outside of tank body 1 of Protein Separation tank is passed through
Polyurethane heat-insulation, a diameter of 3.5m of Protein Separation tank, tank 7.0m high, the affiliated pipeline section product of mozzle 5 is in 0.07 ㎡.Its
Along inlet 3 is higher by middle Protein Separation tank inner guiding pipe 5, its difference in height is 20cm.So, once injection liquefier from leading
Flowed out in flow tube 5, by the shunting of spreader 7, produce eddy flow, slowly moved in tank body 1, while liquefier will once be sprayed
Sink, protein floats；Final protein matter forms floccule on upper strata, and flame filter press is entered into by overfall 3；Once spray
Penetrate liquefier to be flowed out by the underflow outlet 9 of the bottom of tank body 1, the flow of its outflow is 40 cubes ms/h, enters into laminar flow
Pipe, then proceedes to the production process of starch sugar.
The albumen flocculating effect on upper strata is good, and sheet is presented, and is then filtered by high temperature filtration machine again, by being retained after filtering
Solid content it is most of be protein, also contain other a small amount of impurity.These solid contents can be added directly into cornstarch life
Albumen pipe bundle drier during product, by after drying, being sold as commodity egg white powder, its color and luster and albumen powder indifference
Not.Liquid after squeezing is mainly liquid glucose, continue back at once injection liquefier in, circular treatment.
Using the method and apparatus of the present embodiment, will once 70% Separation of Proteins be out in injection liquefier so that
The yield of the albumen powder in whole corn processing production starch sugar improves 0.31%.
Example IV：
Liquefier will be once sprayed to pass through with flow as 45 cubes ms/h after pillar liquefier fully liquefies flocculation
The feed tube 4 of connection inlet 2 and mozzle 5 enters into Protein Separation tank, and the material of Protein Separation tank is SUS304, albumen point
Circular housing 5 is provided that inside the tank body 1 of tank, the gap between the bottom of mozzle 5 and the spreader conical surface is 0.08m's
There is the distance of 0.3m at the top of distance, the top of mozzle 5 and affiliated Protein Separation tank.The outside of tank body 1 of Protein Separation tank is passed through
Polyurethane heat-insulation, a diameter of 4.0m of Protein Separation tank, tank 8.0m high, the affiliated pipeline section product of mozzle 5 is in 0.08 ㎡.Its
Along inlet 3 is higher by middle Protein Separation tank inner guiding pipe 5, its difference in height is 20cm.So, once injection liquefier from leading
Flowed out in flow tube 5, by the shunting of spreader 7, produce eddy flow, slowly moved in tank body 1, while liquefier will once be sprayed
Sink, protein floats；Final protein matter forms floccule on upper strata, and flame filter press is entered into by overfall 3；Once spray
Penetrate liquefier to be flowed out by the underflow outlet 9 of the bottom of tank body 1, the flow of its outflow is 43 cubes ms/h, enters into laminar flow
Pipe, then proceedes to the production process of starch sugar.
The albumen flocculating effect on upper strata is good, and sheet is presented, and is then filtered by high temperature filtration machine again, by being retained after filtering
Solid content it is most of be protein, also contain other a small amount of impurity.These solid contents can be added directly into cornstarch life
Albumen pipe bundle drier during product, by after drying, being sold as commodity egg white powder, its color and luster and albumen powder indifference
Not.Liquid after squeezing is mainly liquid glucose, continue back at once injection liquefier in, circular treatment.
Using the method and apparatus of the present embodiment, will once 72% Separation of Proteins be out in injection liquefier so that
The yield of the albumen powder in whole corn processing production starch sugar improves 0.32%.
Embodiment five：
Liquefier will be once sprayed to pass through with flow as 45 cubes ms/h after pillar liquefier fully liquefies flocculation
The feed tube 4 of connection inlet 2 and mozzle 5 enters into Protein Separation tank, and the material of Protein Separation tank is SUS304, albumen point
Circular housing 5 is provided that inside the tank body 1 of tank, the gap between the bottom of mozzle 5 and the spreader conical surface is 0.08m's
There is the distance of 0.3m at the top of distance, the top of mozzle 5 and affiliated Protein Separation tank.The outside of tank body 1 of Protein Separation tank is passed through
Polyurethane heat-insulation, a diameter of 4.5m of Protein Separation tank, tank 8.5m high, the affiliated pipeline section product of mozzle 5 is in 0.08 ㎡.Its
Along inlet 3 is higher by middle Protein Separation tank inner guiding pipe 5, its difference in height is 20cm.So, once injection liquefier from leading
Flowed out in flow tube 5, by the shunting of spreader 7, produce eddy flow, slowly moved in tank body 1, while liquefier will once be sprayed
Sink, protein floats；Final protein matter forms floccule on upper strata, and flame filter press is entered into by overfall 3；Once spray
Penetrate liquefier to be flowed out by the underflow outlet 9 of the bottom of tank body 1, the flow of its outflow is 43 cubes ms/h, enters into laminar flow
Pipe, then proceedes to the production process of starch sugar.
The albumen flocculating effect on upper strata is good, and sheet is presented, and is then squeezed by flame filter press again, and squeeze pressure control exists
0.5Mpa, the solid content major part by retention after squeezing is protein, also contains other a small amount of impurity.These solid contents can be with
The albumen pipe bundle drier during production of corn starch is added directly into, by after drying, being gone out as commodity egg white powder
Sell, its color and luster and albumen powder indifference.Liquid after squeezing is mainly liquid glucose, continues back in once injection liquefier, follows
Ring treatment.
Using the method and apparatus of the present embodiment, will once 75% Separation of Proteins be out in injection liquefier so that
The yield of the albumen powder in whole corn processing production starch sugar improves 0.32%.
Embodiment six：
Liquefier will be once sprayed to pass through with flow as 48 cubes ms/h after pillar liquefier fully liquefies flocculation
The feed tube 4 of connection inlet 2 and mozzle 5 enters into Protein Separation tank, and the material of Protein Separation tank is SUS304, albumen point
Circular housing 5 is provided that inside the tank body 1 of tank, the gap between the bottom of mozzle 5 and the spreader conical surface is 0.10m's
There is the distance of 0.3m at the top of distance, the top of mozzle 5 and affiliated Protein Separation tank.The outside of tank body 1 of Protein Separation tank is passed through
Polyurethane heat-insulation, a diameter of 5.0m of Protein Separation tank, tank 10.0m high, the affiliated pipeline section product of mozzle 5 is in 0.10 ㎡.
Along inlet 3 is higher by wherein in Protein Separation tank inner guiding pipe 5, its difference in height is 20cm.So, once injection liquefier from
Flowed out in mozzle 5, by the shunting of spreader 7, produce eddy flow, slowly moved in tank body 1, while liquefaction will once be sprayed
Liquid sinks, and protein floats；Final protein matter forms floccule on upper strata, and flame filter press is entered into by overfall 3；Once
Injection liquefier is flowed out by the underflow outlet 9 of the bottom of tank body 1, and the flow of its outflow is 45 cubes ms/h, enters into laminar flow
Pipe, then proceedes to the production process of starch sugar.
The albumen flocculating effect on upper strata is good, and sheet is presented, and is then filtered by high temperature filtration machine again, by being retained after filtering
Solid content it is most of be protein, also contain other a small amount of impurity.These solid contents can be added directly into cornstarch life
Albumen pipe bundle drier during product, by after drying, being sold as commodity egg white powder, its color and luster and albumen powder indifference
Not.Liquid after squeezing is mainly liquid glucose, continue back at once injection liquefier in, circular treatment.
Using the method and apparatus of the present embodiment, will once 77% Separation of Proteins be out in injection liquefier so that
The yield of the albumen powder in whole corn processing production starch sugar improves 0.33%.
Embodiment seven：
Liquefier will be once sprayed to pass through with flow as 48 cubes ms/h after pillar liquefier fully liquefies flocculation
The feed tube 4 of connection inlet 2 and mozzle 5 enters into Protein Separation tank, and the material of Protein Separation tank is SUS304, albumen point
Circular housing 5 is provided that inside the tank body 1 of tank, the gap between the bottom of mozzle 5 and the spreader conical surface is 0.10m's
There is the distance of 0.3m at the top of distance, the top of mozzle 5 and affiliated Protein Separation tank.The outside of tank body 1 of Protein Separation tank is passed through
Polyurethane heat-insulation, a diameter of 5.5m of Protein Separation tank, tank 11.0m high, the affiliated pipeline section product of mozzle 5 is in 0.10 ㎡.
Along inlet 3 is higher by wherein in Protein Separation tank inner guiding pipe 5, its difference in height is 20cm.So, once injection liquefier from
Flowed out in mozzle 5, by the shunting of spreader 7, produce eddy flow, slowly moved in tank body 1, while liquefaction will once be sprayed
Liquid sinks, and protein floats；Final protein matter forms floccule on upper strata, and flame filter press is entered into by overfall 3；Once
Injection liquefier is flowed out by the underflow outlet 9 of the bottom of tank body 1, and the flow of its outflow is 45 cubes ms/h, enters into laminar flow
Pipe, then proceedes to the production process of starch sugar.
The albumen flocculating effect on upper strata is good, and sheet is presented, and is then squeezed by flame filter press again, and squeeze pressure control exists
0.5Mpa, the solid content major part by retention after squeezing is protein, also contains other a small amount of impurity.These solid contents can be with
The albumen pipe bundle drier during production of corn starch is added directly into, by after drying, being gone out as commodity egg white powder
Sell, its color and luster and albumen powder indifference.Liquid after squeezing is mainly liquid glucose, continues back in once injection liquefier, follows
Ring treatment.
Using the method and apparatus of the present embodiment, will once 79% Separation of Proteins be out in injection liquefier so that
The yield of the albumen powder in whole corn processing production starch sugar improves 0.34%.
Embodiment eight：
Liquefier will be once sprayed to pass through with flow as 50 cubes ms/h after pillar liquefier fully liquefies flocculation
The feed tube 4 of connection inlet 2 and mozzle 5 enters into Protein Separation tank, and the material of Protein Separation tank is SUS304, albumen point
Circular housing 5 is provided that inside the tank body 1 of tank, the gap between the bottom of mozzle 5 and the spreader conical surface is 0.10m's
There is the distance of 0.3m at the top of distance, the top of mozzle 5 and affiliated Protein Separation tank.The outside of tank body 1 of Protein Separation tank is passed through
Polyurethane heat-insulation, a diameter of 6.0m of Protein Separation tank, tank 12.0m high, the affiliated pipeline section product of mozzle 5 is in 0.10 ㎡.
Along inlet 3 is higher by wherein in Protein Separation tank inner guiding pipe 5, its difference in height is 20cm.So, once injection liquefier from
Flowed out in mozzle 5, by the shunting of spreader 7, produce eddy flow, slowly moved in tank body 1, while liquefaction will once be sprayed
Liquid sinks, and protein floats；Final protein matter forms floccule on upper strata, and flame filter press is entered into by overfall 3；Once
Injection liquefier is flowed out by the underflow outlet 9 of the bottom of tank body 1, and the flow of its outflow is 48 cubes ms/h, enters into laminar flow
Pipe, then proceedes to the production process of starch sugar.
The albumen flocculating effect on upper strata is good, and sheet is presented, and is then squeezed by flame filter press again, and squeeze pressure control exists
0.5Mpa, the solid content major part by retention after squeezing is protein, also contains other a small amount of impurity.These solid contents can be with
The albumen pipe bundle drier during production of corn starch is added directly into, by after drying, being gone out as commodity egg white powder
Sell, its color and luster and albumen powder indifference.Liquid after squeezing is mainly liquid glucose, continues back in once injection liquefier, follows
Ring treatment.
Using the method and apparatus of the present embodiment, will once 76% Separation of Proteins be out in injection liquefier so that
The yield of the albumen powder in whole corn processing production starch sugar improves 0.33%.
It should be understood that these embodiments are only illustrative of the invention and is not intended to limit the scope of the invention.In addition, it is to be understood that
After the content for having read instruction of the present invention, those skilled in the art can make various changes or modifications to the present invention, these
The equivalent form of value equally falls within the application appended claims limited range.
Claims (9)
1. method for protein isolation during a kind of starch sugar is produced, it is characterised in that：Comprise the following steps：
A. starch milk is once sprayed through injector, is once sprayed liquefier；
B. the once injection liquefier for step a being obtained fully liquefies after flocculation through pillar liquefier, by Protein Separation tank
Inlet is transported to Protein Separation tank and is separated, and the flotation fluid overflow on upper strata is gone out into Protein Separation tank, obtains overflowing liquid；Lower floor
It is underflow liquefier, secondary injection operation is entered into through the underflow outlet of Protein Separation tank, the production of starch sugar is carried out successively；
C. the overflowing liquid for step b being obtained carries out high temperature filtration, obtains liquefier after meringue and filter, and liquefier after filter is flowed back
Continued with to once injection liquefier, meringue drying and processing obtains albumen powder.
2. method for protein isolation during starch sugar as claimed in claim 1 is produced, it is characterised in that：Feed liquor in the step b
The flow quantity that enters of mouth goes out flow quantity more than underflow outlet.
3. method for protein isolation during starch sugar as claimed in claim 1 is produced, it is characterised in that：In the step b once
Injection liquefier enters into the mozzle being arranged on inside the Protein Separation tank by pipeline through the inlet of Protein Separation tank,
Enter in tank body after being shunted through spreader again, be layered, obtain the flotation fluid on upper strata and the underflow liquefier of bottom.
4. method for protein isolation during starch sugar as claimed in claim 1 is produced, it is characterised in that：The Protein Separation tank tank
Inlet and overfall are respectively arranged with body sidewall, the inlet position is higher than the overfall；The bottom of the tank body
It is provided with underflow outlet；It is vertically provided with hollow mozzle in the tank body, the mozzle top end opening, the top is opened
Open height is higher than the feed liquor open height, and the inlet is communicated to the top end opening of the mozzle by feed tube, described
Mozzle lower openings are fixedly attached on support, and the spreader of cone shape is provided with the support, the spreader
Cone corresponds to the center of the mozzle caliber.
5. method for protein isolation during starch sugar as claimed in claim 4 is produced, it is characterised in that：The support is fixedly connected
Onto support bar, the support bar two ends are fixedly attached to inner tank wall both sides, are provided between the support bar and tank base
Distance.
6. method for protein isolation during starch sugar as claimed in claim 4 is produced, it is characterised in that：The cone of the spreader
Corresponding to the center of the mozzle caliber, the conical surface of the spreader is vertical with the mozzle bottom port opening's edge
Distance is 4~10 centimetres.
7. method for protein isolation during starch sugar as claimed in claim 4 is produced, it is characterised in that：The mozzle lower end
Mouth opening's edge is 0.2~0.5 meter with the vertical range of tank base medial surface.
8. method for protein isolation during starch sugar as claimed in claim 4 is produced, it is characterised in that：The mozzle is cylinder
Shape, elliptic cylindrical shape or polyhedral mozzle.
9. method for protein isolation during starch sugar as claimed in claim 4 is produced, it is characterised in that：The tank body outside is set
There is heat-insulation layer.
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| CN109517861A (en) * | 2018-11-19 | 2019-03-26 | 山东盛泰生物科技有限公司 | Method for protein isolation and its separator in a kind of production of starch sugar |
| CN111807592A (en) * | 2020-07-17 | 2020-10-23 | 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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